WO2025191031A1 - Device and method for producing a fluid mixture - Google Patents

Abstract

The invention relates to a device (1) for producing a fluid mixture, comprising: - a first mixing chamber (20) having a first inlet opening (201), via which a first fluid (F₁) can be introduced into the first mixing chamber (20) along a first fluid flow direction (R₁), a second inlet opening (202), via which a second fluid (F₂) can be introduced into the first mixing chamber (20) along a second fluid flow direction (R₂), and an outlet opening (203), via which an intermediate fluid mixture (F₁₂) comprising the first fluid (F₁) and the second fluid (F₂) can be discharged along a fluid mixture flow direction (R₁₂), wherein, upstream of the outlet opening (203), an outlet channel (207) is formed, the cross-sectional area of which defined transversely to the fluid mixture flow direction (R₁₂) decreases along the fluid mixture flow direction (R₁₂) toward the outlet opening (203); - a second mixing chamber (40) having a first inlet opening (401), via which the intermediate fluid mixture (F₁₂) can be introduced into the second mixing chamber (40) along the fluid mixture flow direction (R₁₂), a second inlet opening (402), via which a third fluid (F₃) can be introduced into the second mixing chamber (40) along a third fluid flow direction (R₃), and an outlet opening (403), via which the fluid mixture (F₁₂₃) comprising the first fluid (F₁), the second fluid (F₂) and the third fluid (F₃) can be discharged.

Description

Device and method for producing a fluid mixture

The invention generally relates to a device for generating a fluid mixture and a corresponding method. A fluid mixture can be a mixture of two fluids (liquids), but in the sense of the present application, it can also be a dispersion. A dispersion is a heterogeneous mixture of at least two substances that are insoluble or only slightly soluble in one another. A disperse phase is distributed in a dispersion medium. In the present case, the device and method are used in particular to produce a suspension in which a liquid serves as the dispersion medium and a solid as the disperse phase, or an emulsion in which both the disperse phase and the dispersion medium are liquid.

The invention relates to combining or mixing at least three separate fluids. Depending on the type of fluid used, the process can produce particles that are, for example, distributed in a liquid, creating an overall suspension. The particles can be considered a solid that forms the dispersed phase. In many applications, particles with a small diameter are desirable. Particles in the nanometer size range are also referred to as nanoparticles. These nanoparticles can be relevant in chemical, biochemical, or pharmaceutical processes. The invention particularly relates to a device and a method for producing such nanoparticles or particles in the micrometer range.

An example of suspensions of pharmaceutical importance are liposomally formulated drugs. The particle or vesicle size and the polydispersity index are key physical parameters that influence the therapeutic index of liposomally formulated drugs. It is known that smaller liposomes exhibit slower blood clearance and thus increase the bioavailability of drugs. Therefore, there is a need to be able to produce particles in the pharmaceutically required size with high quality, i.e., with a low polydispersity index. Devices known as microfluidics or microfluidic mixers are known for the generation of nanoparticles. Microfluidic mixers typically have very small microchannels that generate low Reynolds numbers and thus generally laminar flow without significant turbulence, which is unfavorable for fluid mixing. The flow channels are quite long relative to their cross-sectional dimensions. These channels are expensive to manufacture and can easily become clogged during operation. Furthermore, their use in mass production can be difficult or even impossible.

The present invention is based on the object of creating a device and a method for generating a fluid mixture (with nanoparticles with a specific particle size and defined size distribution) that are as minimally susceptible to failure as possible. In particular, the object is also to create a device and a method that can be used both on a laboratory scale (i.e., a few nanoliters per minute) and in mass production (i.e., several liters per minute).

This object is achieved according to the invention by a device having the features of claim 1. Embodiments of the invention are specified in the subclaims.

According to this, the device for generating a fluid mixture initially comprises a first mixing chamber with a first inlet opening, via which a first fluid can be introduced into the first mixing chamber along a first fluid flow direction, a second inlet opening, via which a second fluid can be introduced into the first mixing chamber along a second fluid flow direction, and an outlet opening, via which an intermediate fluid mixture comprising the first fluid and the second fluid can be discharged along a fluid mixture flow direction. (Immediately) upstream of the outlet opening, an outlet channel is formed, the cross-sectional area of which, defined transversely to the fluid mixture flow direction, decreases along the fluid mixture flow direction towards the outlet opening. The outlet channel forms a downstream end section of the first mixing chamber. The outlet channel makes it possible to prevent the formation of so-called dead water regions in the first mixing chamber.

Furthermore, the device comprises a second mixing chamber with a first inlet opening, via which the intermediate fluid mixture can be introduced into the second mixing chamber along the fluid mixture flow direction, a second inlet opening, via which a third fluid can be introduced into the second mixing chamber (stationary) can be introduced, and an outlet opening through which the fluid mixture comprising the first fluid, the second fluid, and the third fluid can be discharged. The second mixing chamber is thus arranged downstream of the first mixing chamber, wherein the first mixing chamber and the second mixing chamber are fluidically connected such that the intermediate fluid mixture exiting the outlet opening of the first mixing chamber enters the second mixing chamber via its first inlet opening.

Supply devices can be provided for introducing the fluids into the mixing chambers. Specifically, the device comprises a first supply device that is fluidically connected to the first mixing chamber via the first inlet opening and is configured to direct the first fluid into the first mixing chamber along the first fluid flow direction (variable in time and space).

The first supply device comprises a fluidic component having an outlet opening fluidically connected to the first inlet opening of the first mixing chamber. In particular, the outlet opening of the fluidic component can correspond to the first inlet opening of the first mixing chamber.

The fluidic component comprises at least one means for the targeted change of direction of the first fluid flowing through the fluidic component. For the targeted change of direction, alternating vortices, e.g., generated by colliding fluid flows within the fluidic component or by a disruptive body within the fluidic component, can be used. With this type of means for generating the targeted change of direction, sufficient space must be provided for the generation and subsequent dissipation of the vortex structures. In particular, this at least one means is provided and designed to create a spatial oscillation of the first fluid at the outlet opening. In one embodiment, the means for the targeted change of direction of the first fluid can be designed to bring about an oscillation of the first fluid in an oscillation plane.

The first fluid is thus not fed into the first mixing chamber as a (quasi)stationary flow, but as an oscillating fluid flow that moves periodically and changes over time. In addition to a longitudinal flow component along the first fluid flow direction, the first fluid also has a lateral flow component (transverse to the first fluid flow direction) that changes over time. This can generate turbulence in the first mixing chamber, so that a high mixing quality can be achieved. Accordingly, the first fluid enters the first mixing chamber from the first supply device in a vibrating or dynamic manner. As a result, the first fluid receives a constantly changing flow velocity component perpendicular to its main flow direction (lateral flow component or first fluid flow direction).

The device further comprises a first interaction channel arranged between the first mixing chamber and the second mixing chamber. The first interaction channel connects the outlet opening of the first mixing chamber and the first inlet opening of the second mixing chamber and has a cross-sectional area transverse to the fluid mixture flow direction, which is constant at least over a section immediately downstream of the outlet opening of the first mixing chamber. Accordingly, the outlet opening of the first mixing chamber or the inlet opening of the first interaction channel represents the downstream end of the outlet channel. Since the cross-sectional area of the outlet channel decreases along the fluid mixture flow direction toward the outlet opening, the cross-sectional area of the outlet channel is smallest at the outlet opening of the first mixing chamber or at the inlet opening of the first interaction channel. This position is further characterized in that it forms the upstream end of a section (of the first interaction channel) with a constant cross-sectional area.

For example, the first interaction channel in said section can be tubular. The first interaction channel can have a length that is at least three times its width at the level of the outlet opening of the first mixing chamber. The length is the extent of the first interaction channel along the fluid mixture flow direction from the outlet opening of the first mixing chamber to the first inlet opening of the second mixing chamber. The width is the extent of the first interaction channel in the oscillation plane perpendicular to the fluid mixture flow direction.

The first interaction channel can serve to continue the mixing process downstream of the outlet opening of the first mixing chamber; and if particles are generated during the mixing process, these can grow in the first interaction channel (controlled by the length of the first interaction channel). The section of the first interaction channel with a constant cross-sectional area has the effect that the intermediate fluid mixture initially remains as undisturbed as possible in order to achieve a defined Reaction time for the intermediate fluid mixture without flow separation effects and simultaneous homogenization of the flow.

According to one embodiment, the first interaction channel extends at least partially along a longitudinal axis, which is in particular parallel to the fluid mixture flow direction. The first interaction channel can also (alternatively or additionally) have a meandering section. The curvature(s) caused by the meandering shape can prevent the formation of so-called dead water areas.

In addition, the first interaction channel may have a section in which the cross-sectional area increases downstream transverse to the fluid mixture flow direction.

The transition between the first interaction channel and the second mixing chamber (i.e., the position of the outlet opening of the first interaction channel or the first inlet opening of the second mixing chamber) can be characterized by a sudden increase in the cross-sectional area (transverse to the fluid mixture flow direction). The second inlet opening of the second mixing chamber can be arranged in the region of the sudden increase in the cross-sectional area.

Furthermore, the device comprises a second supply device which is fluidically connected to the first mixing chamber via the second inlet opening and is designed to guide the second fluid along the second fluid flow direction into the first mixing chamber, and a third supply device which is fluidically connected to the second mixing chamber via the second inlet opening and is designed to guide the third fluid along the third fluid flow direction into the second mixing chamber.

The third fluid flow direction, i.e., the fluid flow direction in which the third fluid enters the second mixing chamber, and the fluid mixture flow direction, i.e., the direction in which the intermediate fluid mixture of the first and second fluid enters the second mixing chamber, can enclose an angle of less than or equal to 90°. This limits the shear rate of the fluids in the second mixing chamber. Particles present in the intermediate fluid mixture thus experience the lowest possible mechanical stress when they come into contact with the third fluid. Accordingly, damage to the particles or agglomeration/aggregation of the particles through fusion or sticking of the particles can be avoided. This has a positive effect on the polydispersity index of the particles. To enhance this effect, it is advantageous to The velocity values of the third fluid and the intermediate fluid mixture should be chosen to be very similar. This can be achieved by selecting suitable process parameters. With the device according to the invention and the method described below, the particles mentioned above can be produced in the pharmaceutically required size with high quality, i.e., with a low polydispersity index.

Preferably, the angle between the fluid mixture flow direction and the third fluid flow direction is less than 45°, and in particular is between 5° and 40°. The smaller this angle, the lower the shear rate of the fluids.

According to one embodiment, the third supply device is provided and configured to conduct the third fluid as a (quasi-)stationary flow into the second mixing chamber. This also limits the shear rate of the fluids in the second mixing chamber. The second supply device can also be provided and configured to conduct the second fluid as a (quasi-)stationary flow into the first mixing chamber.

The third supply device has a supply channel that extends along the third fluid flow direction and opens into the second inlet opening of the second mixing chamber. The supply channel has, in particular, a rectilinear shape. The supply channel, or its shape, largely determines the fluid flow direction for the third fluid upon entry into the second mixing chamber.

The means for deliberately changing the direction of the first fluid is designed to cause the first fluid to oscillate in an oscillation plane. The supply channel extends in a plane that is parallel to or corresponds to the oscillation plane. As a result, the intermediate fluid mixture and the third fluid move in a common plane.

As already mentioned, the fluidic component comprises at least one means for deliberately changing the direction of the first fluid flowing through the fluidic component. This configuration of the first supply device brings about the targeted change in direction of the first fluid, so that the first fluid moves within the first mixing chamber in a temporally variable manner, wherein the first fluid has a movement component along the first fluid flow direction and a movement component transverse to the first fluid flow direction. According to one embodiment, the fluidic component comprises a flow chamber which, in addition to the aforementioned outlet opening, also has an inlet opening and through which the first fluid can flow, entering the flow chamber through the inlet opening and exiting the flow chamber through the outlet opening. According to one embodiment, the inlet opening and the outlet opening of the fluidic component can have different widths. In particular, the flow chamber has a main flow channel that connects the inlet opening of the flow chamber (or of the fluidic component) and the outlet opening of the flow chamber (or of the fluidic component), and at least one secondary flow channel as a means for deliberately changing the direction of the first fluid. Moving components for generating the oscillation can be dispensed with in the fluidic component, thus eliminating the associated costs and expenditures. Furthermore, by omitting moving components, vibration and noise development are relatively low.

As a means for deliberately changing the direction of the first fluid, the flow chamber can have the aforementioned at least one bypass channel. A portion of the first fluid, the bypass flow, can flow through the bypass channel. The portion of the first fluid that does not enter the bypass channel but exits the fluidic component is referred to as the main flow. The at least one bypass channel can have an inlet located near the outlet opening of the fluidic component and an outlet located near the inlet opening of the fluidic component. The at least one bypass channel can be arranged next to (not behind or in front of) the main flow channel, viewed along the first fluid flow direction (from the inlet opening to the outlet opening). In particular, two bypass channels can be provided which extend laterally next to the main flow channel (viewed along the first fluid flow direction), wherein the main flow channel is arranged between the two bypass channels. According to a preferred embodiment, the secondary flow channels and the main flow channel are arranged in a row transverse to the first fluid flow direction and each extend along the first fluid flow direction.

Preferably, the at least one secondary flow channel is separated from the main flow channel by a block. This block can have different shapes. For example, the cross section of the block can taper along the first fluid flow direction (from the inlet opening to the outlet opening). In addition, the block can have rounded edges. Sharp edges may be provided on the block, particularly near the inlet and/or outlet ports.

According to one embodiment, the at least one secondary flow channel can have a greater or lesser depth than the main flow channel. (The depth is the extent transverse to the oscillation plane of the first fluid.) This makes it possible to influence the oscillation frequency of the first fluid exiting the fluidic component. By reducing the component depth in the region of the at least one secondary flow channel (compared to the main flow channel), the oscillation frequency decreases if the other parameters remain essentially unchanged. Accordingly, the oscillation frequency increases if the component depth in the region of the at least one secondary flow channel is increased (compared to the main flow channel) and the other parameters remain essentially unchanged.

A further possibility for influencing the oscillation frequency of the first fluid exiting the fluidic component can be created by at least one separator, which is preferably provided at the inlet of the at least one bypass channel. The separator supports the separation of the bypass flow from the flow of the first fluid. A separator is understood to be an element that projects into the flow chamber at the inlet of the at least one bypass channel (transverse to the flow direction prevailing in the bypass channel). The separator can be provided as a deformation (in particular an indentation) of the bypass channel wall or as a projection of another design. For example, the separator can be (circular) conical or pyramidal. The use of such a separator makes it possible not only to influence the oscillation frequency but also to vary the so-called oscillation angle. The oscillation angle is the angle covered by the oscillating fluid jet (between its two maximum deflections). If several bypass channels are provided, a separator can be provided for each of the bypass channels or only for some of the bypass channels.

The cross-sectional area of the inlet and outlet openings of the fluidic component (but also of the first mixing chamber and the second mixing chamber) can have any shape, such as square, rectangular, polygonal, round, oval, etc.

According to one embodiment, the first supply device and the first inlet opening of the first mixing chamber on the one hand and the second supply device and the second inlet opening of the first mixing chamber, on the other hand, are arranged relative to one another such that the first fluid flow direction and the second fluid flow direction enclose an angle of 45° to 90° in a plane parallel to the first fluid flow direction. An angle of substantially 45° is particularly preferred. This can positively influence the mixing quality and the mixing path length, or rather, the mixing duration. For manufacturing reasons, the angle can also be substantially 90°.

If the means for deliberately changing the direction of the first fluid is designed to cause the first fluid to oscillate in an oscillation plane, the second supply device and the second inlet opening of the first mixing chamber can be arranged such that the second fluid flow direction and the oscillation plane of the first fluid enclose an angle of 30° to 150° in a plane transverse to the first fluid flow direction. This angle is preferably substantially 90°.

With regard to the second supply device, it can be provided that it is designed and configured to conduct the second fluid as a (quasi-)stationary flow into the first mixing chamber. For example, the second supply device can be designed as a tube whose longitudinal axis (or its downstream elongated end section) determines the second fluid flow direction of the second fluid. By means of a pumping device, the second fluid can be conducted through the tube and the second inlet opening into the first mixing chamber.

Alternatively, the second supply device (like the first supply device) can also comprise a fluidic component. This fluidic component can operate according to the same principle as the fluidic component of the first supply device. For example, it can have at least one means for deliberately changing the direction of the second fluid flowing through the fluidic component, in particular for generating a spatial oscillation of this fluid at the outlet opening. The other features of the fluidic component of the first supply device can also be transferred to the fluidic component of the second supply device. Thus, a first oscillating fluid and a second oscillating fluid meet in the first mixing chamber. The fluidic component of the second supply device can have a smaller oscillation angle than the fluidic component of the first supply device. Both oscillation angles can also be the same. The first mixing chamber can have a longitudinal axis that is defined such that it extends along the first fluid flow direction or the fluid mixture flow direction. According to one embodiment, the cross-sectional area of the first mixing chamber increases transversely to the longitudinal axis along the longitudinal axis in at least one section. For example, starting from the first inlet opening of the first mixing chamber in an upstream end section of the first mixing chamber, the cross-sectional area can increase with increasing distance from the first inlet opening. The upstream end section can thus form an inlet channel (widening downstream) of the first mixing chamber. The outlet channel can be directly connected to the inlet channel. Alternatively, an intermediate section of the first mixing chamber can be provided between the inlet channel and the outlet channel, in which intermediate section the cross-sectional area of the first mixing chamber is essentially constant.

If the means for deliberately changing the direction of the first fluid is designed to cause the first fluid to oscillate in an oscillation plane, the extent of the first mixing chamber in the oscillation plane and transversely to the longitudinal axis, starting from the first inlet opening of the first mixing chamber in the inlet channel, can increase with increasing distance from the first inlet opening, or the extent of the first mixing chamber in the oscillation plane and transversely to the longitudinal axis in the outlet channel can decrease with increasing distance from the first inlet opening. In particular, this extent of the first mixing chamber can also increase (immediately) downstream of the second inlet opening of the first mixing chamber in the inlet channel. In the inlet channel, the boundary walls of the first mixing chamber (viewed in the oscillation plane) thus enclose an angle that is preferably oriented towards the oscillation angle of the oscillating first fluid. This angle can be up to 10° smaller or up to 10° larger than the oscillation angle, or can assume a value between these two values. It is particularly preferred if this angle is up to 5° smaller or up to 5° larger than the oscillation angle, or can assume a value between these two values. This prevents the oscillation of the first fluid in the first mixing chamber from being adversely affected. The oscillation angle of the first fluid can be at least 5°, preferably at least 25°, particularly preferably at least 40°. For many applications, an oscillation angle between 25° and 50°, in particular between 30° and 45°, is suitable. A typical maximum value for the oscillation angle is 75°. The boundary walls of the first mixing chamber (viewed in the oscillation plane) also close in the outlet channel. an angle that is preferably smaller than the angle between the boundary walls of the first mixing chamber in the inlet channel. Particularly preferably, the angle of the outlet channel is up to 15° smaller than the angle of the inlet channel. In addition, the extent of the first mixing chamber transverse to the oscillation plane in the inlet channel can increase with increasing distance from the first inlet opening, or the extent of the first mixing chamber transverse to the oscillation plane in the outlet channel can decrease with increasing distance from the first inlet opening.

The (relative) size of the inlet and outlet channels of the first mixing chamber can be designed depending on the application.

According to one embodiment, the second inlet opening of the first mixing chamber is offset downstream from the first inlet opening of the first mixing chamber along the longitudinal axis of the first mixing chamber. Preferably, the second inlet opening is formed within the inlet channel (i.e., in a boundary wall of the inlet channel). Viewed along the longitudinal axis, the distance between the first and second inlet openings can correspond to at least half the width of the first inlet opening of the first mixing chamber, wherein the width is defined parallel to the oscillation plane of the first fluid and transverse to the longitudinal axis of the first mixing chamber.

The first inlet opening and the outlet opening of the first mixing chamber can be formed on opposite sides of the first mixing chamber. Thus, the first inlet opening can form the upstream end of the first mixing chamber, and the outlet opening the downstream end. In particular, the first inlet opening and the outlet opening can be located on the longitudinal axis. The first inlet opening and the outlet opening can be defined where the cross-sectional area of the first mixing chamber is smallest, transverse to its longitudinal axis, through which the incoming first fluid and the outgoing intermediate fluid mixture pass, respectively.

Furthermore, it is conceivable that the first mixing chamber has a volume that is larger than the volume of the fluidic component or the flow chamber of the fluidic component. In particular, both the width (extension transverse to the longitudinal axis of the first mixing chamber and in the oscillation plane of the first fluid) and the length (extension along the longitudinal axis) of the first mixing chamber can be be greater than the width (extension transverse to the first fluid flow direction and in the oscillation plane of the first fluid) or length (extension along the first fluid flow direction) of the flow chamber of the fluidic component. This volume ratio can prevent an undesirably high pressure from building up in the first mixing chamber. Alternatively, the volume of the first mixing chamber can be smaller than the volume of the flow chamber of the fluidic component. In this case, the width and/or length of the first mixing chamber can be smaller than the width or length of the flow chamber of the fluidic component.

Analogous to the first interaction channel, a second interaction channel can be connected downstream of the outlet opening of the second mixing chamber.

The second mixing chamber and/or the second interaction channel each extend along an axis corresponding to the flow direction of the generated fluid mixture. This axis each forms an angle with the third fluid flow direction and the fluid mixture flow direction (of the intermediate fluid mixture). According to one embodiment, the angle between the axis and the third fluid flow direction and the angle between the axis and the fluid mixture flow direction are different (in the oscillation plane). In particular, the angle between the axis and the third fluid flow direction can be greater than the angle between the axis and the fluid mixture flow direction. Both angles are preferably less than 180°. For example, the angle between the axis and the third fluid flow direction can be 170° to 179°. For example, the angle between the axis and the fluid mixture flow direction can be 160° to 169°. The angle between the axis and the third fluid flow direction, the angle between the axis and the fluid mixture flow direction, and a further angle between the fluid mixture flow direction and the third fluid flow direction add up to 360°.

When using the device, for example in a method for producing a fluid mixture described below, the volume flows of the first, second and third fluids can be selected such that the resulting velocity vector of the intermediate fluid mixture at the first inlet opening of the second mixing chamber and the resulting velocity vector of the third fluid at the second inlet opening of the second mixing chamber are in sum such that the resulting velocity vector of the fluid mixture is parallel to the axis of the second mixing chamber or the second interaction channel. Thus, the angle between the velocity vector of the fluid mixture and the third fluid flow direction (the velocity vector of the third fluid) can be 170° to 179°. Furthermore, the angle between the velocity vector of the fluid mixture and the fluid mixture flow direction (the velocity vector of the intermediate fluid mixture) can be 160° to 169°.

The first, second, and third fluids can be supplied to the first, second, and third supply devices, respectively, by means of a pumping device. For example, the pumping devices can be designed as syringe pumps or circulation pumps. HPLC pumps or diaphragm pumps can be used as alternatives to syringe pumps.

The device presented here for generating a fluid mixture has so far been described with a first mixing chamber and a second mixing chamber. However, it is conceivable that the device comprises at least one further mixing chamber with a corresponding supply device. The at least one further mixing chamber can be arranged according to the described principle, so that the first inlet opening of the nth mixing chamber is fluidly connected to the outlet opening of the (n-1)th mixing chamber. This results in a cascade-like arrangement of the n mixing chambers.

The object explained at the outset is also achieved by a device having the features of claim 9.

According to this, the device for generating a fluid mixture initially comprises a first mixing chamber with a first inlet opening, via which a first fluid can be introduced into the first mixing chamber along a first fluid flow direction, a second inlet opening, via which a second fluid can be introduced into the first mixing chamber along a second fluid flow direction, and an outlet opening, via which an intermediate fluid mixture comprising the first fluid and the second fluid can be discharged along a fluid mixture flow direction. The device further comprises a second mixing chamber with a first inlet opening, via which the intermediate fluid mixture can be introduced into the second mixing chamber along the fluid mixture flow direction, a second inlet opening, via which a third fluid can be introduced into the second mixing chamber along a third fluid flow direction, and an outlet opening, via which the fluid mixture comprising the first fluid, the second fluid and the third fluid is dischargeable. The second mixing chamber is thus arranged downstream of the first mixing chamber, wherein the first mixing chamber and the second mixing chamber are fluidically connected such that the intermediate fluid mixture exiting the outlet opening of the first mixing chamber (directly) enters the second mixing chamber via its first inlet opening.

Supply devices can be provided for introducing the fluids into the mixing chambers. Specifically, this device also comprises a first supply device that is fluidically connected to the first mixing chamber via the first inlet opening and is configured to conduct the first fluid into the first mixing chamber along the first fluid flow direction.

Furthermore, a second supply device which is fluidically connected to the first mixing chamber via the second inlet opening and is designed to guide the second fluid along the second fluid flow direction into the first mixing chamber, and a third supply device which is fluidically connected to the second mixing chamber via the second inlet opening and is designed to guide the third fluid along the third fluid flow direction into the second mixing chamber can be provided.

The first supply device comprises a fluidic component. The fluidic component comprises an outlet opening fluidically connected to the first inlet opening of the first mixing chamber, and at least one means for selectively changing the direction of the first fluid flowing through the fluidic component, in particular for forming a spatial oscillation of the first fluid at the outlet opening.

The device is characterized in that the first inlet opening of the second mixing chamber has a cross-sectional area transverse to the fluid mixture flow direction that is smaller than the cross-sectional area of the second inlet opening of the second mixing chamber. The cross-sectional area of the second inlet opening of the second mixing chamber is defined transversely to the third fluid flow direction. Alternatively or additionally, the device is characterized in that the sum of the cross-sectional area of the first inlet opening of the second mixing chamber and the cross-sectional area of the second inlet opening of the second mixing chamber is similar in size (if the third fluid flow direction and the fluid mixture flow direction lie in one plane) or (if the third fluid flow direction and the fluid mixture flow direction do not lie in one plane) is greater than the cross-sectional area of the outlet opening of the second mixing chamber. Consequently, the average velocity of the intermediate Fluid mixture at the first inlet opening of the second mixing chamber is greater than the average velocity of the third fluid at the second inlet opening of the second mixing chamber. This results in the fluid-mechanical effect that the momentum of the intermediate fluid mixture upon entering the second mixing chamber is greater than the momentum of the third fluid stream upon entering the second mixing chamber. This momentum difference enables the fluid mixture flow direction at the first inlet opening of the second mixing chamber and the third fluid flow direction at the second inlet opening of the second mixing chamber to enclose a relatively large angle, for example 90°, without any significant shearing of the intermediate fluid mixture in the second mixing chamber occurring. The option of choosing 90° for the aforementioned angle allows the second mixing chamber in the region of the second inlet opening, as well as the third feed device, to be designed with a simple structure.

Possible configurations and embodiments of the fluidic component have already been described above. Here, too, the means for deliberately changing the direction of the first fluid can be designed to cause the first fluid to oscillate in an oscillation plane.

According to one embodiment, the second mixing chamber has a constant extension parallel to the oscillation plane and transverse to the fluid mixture flow direction. This extension can be referred to as the width of the second mixing chamber. The width of the second mixing chamber can be constant over its entire length (extension along the fluid mixture flow direction).

It is also conceivable for the second mixing chamber to have an extension parallel to the oscillation plane and transverse to the fluid mixture flow direction that is equal to the extension parallel to the oscillation plane and transverse to the fluid mixture flow direction of the outlet opening of the first mixing chamber and/or the first inlet opening of the second mixing chamber. Furthermore, the first inlet opening and the outlet opening of the second mixing chamber can have the same width, which, for example, corresponds to the width of the second mixing chamber. This can also simplify the structural design of the second mixing chamber.

According to one embodiment, the second mixing chamber has an extension transverse to the oscillation plane that is greater than the extension of the first inlet opening of the second mixing chamber transverse to the oscillation plane. The extension transverse to The oscillation plane can be referred to as depth. Accordingly, the depth of the second mixing chamber can be greater than the depth of the first inlet opening of the second mixing chamber. The depth of the second mixing chamber can be constant over its entire length (extension along the fluid mixture flow direction). In particular, the cross-sectional area (transverse to the fluid mixture flow direction) of the first inlet opening of the second mixing chamber can be smaller than the cross-sectional area (transverse to the fluid mixture flow direction) of the second mixing chamber. The cross-sectional change can be abrupt and, for example, realized by a stepped shape that abruptly changes the depth. Such a stepped shape can lead to the formation of recirculation regions (also called dead water regions) in the second mixing chamber immediately downstream of the first inlet opening and thus impair the function of the second mixing chamber. However, the second inlet opening can be arranged immediately downstream of the first inlet opening, i.e., in a region of potential recirculation regions, so that the third fluid flows through the potential recirculation regions. As a result, the residence time of the third fluid in the second mixing chamber may be indeterminate, but not that of the intermediate fluid mixture, so that ultimately the function of the second mixing chamber is not impaired.

According to one embodiment, a first interaction channel is arranged between the first mixing chamber and the second mixing chamber, connecting the outlet opening of the first mixing chamber and the first inlet opening of the second mixing chamber. The first interaction channel has a cross-sectional area transverse to the fluid mixture flow direction, which is constant at least in some sections. In particular, the cross-sectional area of the first interaction channel can be smaller than the cross-sectional area of the second mixing chamber. The depth (extension transverse to the oscillation plane) of the first interaction channel can be less than the depth of the second mixing chamber, while their widths (extension parallel to the oscillation plane and transverse to the fluid mixture flow direction) can be the same. In particular, the depth of the second mixing chamber can be (constant and) twice the depth of the first interaction channel (in a section immediately upstream of the second mixing chamber). The ratio of the depths (first interaction channel / second mixing chamber) to each other can be based on the ratio of the volume flow of the intermediate fluid mixture to the sum of the volume flows within the second mixing chamber. Preferably, the ratio of the depths (first interaction channel / second mixing chamber) corresponds to the Ratio of volume flows (intermediate fluid mixture / (intermediate fluid mixture + third fluid)).

According to one embodiment, the depth (extension transverse to the oscillation plane) of the first interaction channel is less than the width (extension parallel to the oscillation plane and transverse to the fluid mixture flow direction) of the first interaction channel. The ratio of width to depth can be in a range between 1.5 and 100, preferably between 2 and 10.

The first interaction channel can have a length that is at least three times its width at the level of the outlet opening of the first mixing chamber. The length is the extent of the first interaction channel along the fluid mixture flow direction from the outlet opening of the first mixing chamber to the first inlet opening of the second mixing chamber. The width is the extent of the first interaction channel in the oscillation plane transverse to the fluid mixture flow direction.

The transition between the first interaction channel and the second mixing chamber (i.e., the position of the outlet opening of the first interaction channel or the first inlet opening of the second mixing chamber) can be characterized by a sudden change in the cross-sectional area (transverse to the fluid mixture flow direction). For example, the depth and/or width can change abruptly at the transition.

The transition between the first mixing chamber and the first interaction channel (i.e. the position of the outlet opening of the first mixing chamber or the inlet opening of the first interaction channel) can be defined by arranging a section (outlet channel of the first mixing chamber) immediately upstream, the cross-sectional area of which decreases along the fluid mixture flow direction in the direction of the outlet opening, wherein the cross-sectional area is smallest at the outlet opening of the first mixing chamber or at the inlet opening of the first interaction channel.

To keep the design as simple as possible, the first interaction channel can extend along a longitudinal axis that is particularly parallel to the first fluid flow direction or the fluid mixture flow direction. However, it is also conceivable for the first interaction channel to comprise a meandering section. It is also conceivable that a second interaction channel is connected to the outlet opening of the second mixing chamber.

Configurations of the first supply device, the second supply device and the first mixing chamber have already been described above in connection with other embodiments and can also be transferred to the embodiments in which the first inlet opening of the second mixing chamber has a smaller cross-sectional area than the second inlet opening of the second mixing chamber.

The device according to the invention can be manufactured using machining or subtractive manufacturing processes, replicative processes, for example, injection molding, or additive processes (3D printing). Processes with specific cutting edges (e.g., milling) or subtractive processes (e.g., spark erosion) are also suitable for manufacturing.

The device according to the invention can be manufactured from a variety of materials. Possible materials include plastics (PEEK, PVDF, COC), metals or alloys (stainless steel, aluminum), glass, or ceramic.

The invention further relates to a method for producing a fluid mixture. The method is carried out using the device according to the invention. To carry out the method, a device according to the invention according to one of the embodiments described here, a first fluid, a second fluid, and a third fluid are first provided. The first fluid is introduced into the first mixing chamber at a first volume flow via the first supply device. Simultaneously, the second fluid is introduced into the first mixing chamber at a second volume flow via the second supply device, and the third fluid is introduced into the second mixing chamber at a third volume flow via the third supply device.

In the first mixing chamber, the first and second fluids are given the opportunity to mix, thereby forming an intermediate fluid mixture (with particles). The formation of (nano)particles can be achieved by changing the solubility of substances dissolved in the second fluid through contact/dilution of the second fluid with the first fluid. Nanoparticles are precipitated by nanoprecipitation. Due to the design of the first supply device, which causes spatial oscillation of the first fluid, the velocities or Velocity differences between the first and second fluids in the first mixing chamber are significant, resulting in turbulent mixing. The residence time of the two fluids in the first mixing chamber can vary depending on the application.

In the second mixing chamber, the intermediate fluid mixture generated in the first mixing chamber and the third fluid are combined. Due to the design of the second mixing chamber in the region of its first and second inlet openings, the shear rates in the second mixing chamber are low, so that, in particular, turbulent mixing (rather, quasi-laminar mixing) does not occur in the second mixing chamber. This allows the mechanical stress on the particles to be kept as low as possible. The mixing process in the second mixing chamber serves to stabilize particles of the intermediate fluid mixture.

The size and size distribution of the particles can be influenced by the volume flow rates of the first and second fluids, the oscillation frequency of the first oscillating fluid, and the geometry of the first and second mixing chambers. The width (extension in the oscillation plane and perpendicular to the first fluid flow direction/fluid mixture flow direction) plays a particularly important role. The oscillation frequency of the oscillating first fluid can be at least 100 Hz, typically over 2000 Hz.

Subsequently, the fluid mixture comprising the first fluid, the second fluid and the third fluid is discharged from the second mixing chamber via its outlet opening.

According to one embodiment, the volume flows are set such that the first volume flow is greater than the second volume flow or that the first volume flow and the second volume flow are the same. As far as the second mixing chamber is concerned, the third volume flow can be set such that the volume flow with which the intermediate fluid mixture enters the second mixing chamber is greater than the third volume flow or is the same as the third volume flow. Depending on the application, however, the third volume flow can also be greater than the volume flow with which the intermediate fluid mixture enters the second mixing chamber. The volume flow of the intermediate fluid mixture results from the volume flows of the first and the second fluid. It is conceivable that the first volume flow, the second volume flow and the third volume flow are each constant over the duration of the mixing process. The volume flow of the first, second, and third fluids can be controlled by pumping devices that pump the first, second, and third fluids via the first, second, and third supply devices into the first and second mixing chambers, respectively. Depending on the application, the pressure of the introduced fluids can range from a few millibars (mbar) to several hundred bar (relative to ambient pressure). For applications in the mass production of (lipid) nanoparticles, the inlet pressure can be between 1 and 50 bar, preferably between 1 and 25 bar, particularly preferably between 1 and 10 bar. For the production of emulsions, the pressure can be several hundred bar. A pressure range between 2 and 500 bar is preferred. A pressure range between 10 and 250 bar is particularly preferred.

For application of the process on an industrial scale, the introduction of the first fluid into the first mixing chamber, the introduction of the second fluid into the first mixing chamber and the introduction of the third fluid into the second mixing chamber can each be carried out continuously.

According to one embodiment, the method is carried out using a liquid or a suspension as the first fluid. The second fluid is also either a liquid or a suspension. In the case of suspensions, the two fluids can differ (exclusively) in particle size, for example. Due to the turbulence prevailing in the first mixing chamber, in the case of identical suspensions (as the first and second fluids), the size of the particles in the suspension can be varied, for example. This can also influence the size distribution of the particles.

In general, the first fluid and the second fluid can be different or identical with regard to chemical composition and/or concentration of individual components. For example, the first fluid can comprise an aqueous buffer solution and the second fluid a polymer, a pharmaceutically active ingredient, a polymer-drug conjugate, or a lipid, each in a solvent. The aqueous buffer solution (first fluid) can be, for example, acetate, citrate, phosphate, or TRIS buffer. The buffer solution can contain one or more nucleic acids (DNA, RNA, or mRNA). The buffer solution can have a pH of 3 to 7, preferably 3 to 6. The aqueous solution (first fluid) can further contain surface-active substances such as polyaxamers, polyvinyl alcohols. The solvent of the second fluid can be water-miscible (e.g. ethanol, acetonitrile, acetone) or water-insoluble (e.g. ethyl acetate, chloroform).

It is conceivable that the first fluid is a suspension comprising a solvent and a nucleic acid. The second fluid may comprise a lipid mixture and be suitable for enclosing the nucleic acid of the first fluid during the mixing process and acting as a carrier or vehicle for the nucleic acid in the resulting intermediate fluid mixture. The nucleic acid may be DNA, RNA, or mRNA.

The first fluid and the third fluid may be identical or different with regard to chemical composition and/or concentration of individual components.

Depending on the application, the third fluid can have a specific function. For example, the third fluid can be used to adjust the pH, particle density, or solvent content in the intermediate fluid mixture and/or contain a surfactant.

In general, the chemical composition of the fluids used also determines the particle size of the particles in the produced fluid mixture. At the first inlet opening of the first mixing chamber, the oscillating first fluid has a Reynolds number Re of more than 500, preferably more than 1000, particularly preferably more than 2000. At the first inlet opening of the second mixing chamber, the intermediate fluid mixture has a Reynolds number Re of more than 50, preferably more than 100, particularly preferably more than 200. The Reynolds number Re is determined according to Re = (Ui x hi)/v, where Ui is the flow velocity at the respective inlet opening, hi is the height or depth of the respective inlet opening, and v is the kinematic viscosity of the fluid (mixture).

The process can be used to produce lipid nanoparticles, polymer nanoparticles or liposomes.

The invention will be explained in more detail below using exemplary embodiments in conjunction with the drawings.

They show: Fig. 1 shows a cross section through a device for producing a fluid mixture according to an embodiment;

Fig. 2 shows a cross section through a section of a device for producing a fluid mixture according to a further embodiment, the section showing in particular a first mixing chamber and a first supply device;

Fig. 3-5 a sectional view of the device from Figure 2 along the lines A'-A", B'-B" and C'-C" respectively;

Fig. 6 shows a cross section through a device for producing a fluid mixture according to a further embodiment;

Fig. 7 Deflection of the oscillating first fluid as a function of time upon entry into the first mixing chamber of the device generating a fluid mixture;

Fig. 8 shows a cross section through a device for producing a fluid mixture according to a further embodiment;

Fig. 9 shows a cross section through a device for producing a

Fluid mixture according to another embodiment;

Fig. 10 shows a cross section through a device for producing a

Fluid mixture according to another embodiment;

Fig. 11 is a sectional view of the device of Figure 10 along the lines D‘- D“;

Fig. 12 is a schematic representation of a second mixing chamber according to a further embodiment; and

Fig. 13 is a schematic representation of a method for producing a fluid mixture. The devices and their components shown in the figures are not drawn to scale. Other combinations of the illustrated embodiments are also possible.

Figure 1 schematically shows a device 1 for producing a fluid mixture according to an embodiment of the invention.

The device 1 comprises a first mixing chamber 20, a first interaction channel 30, a second mixing chamber 40, a second interaction channel 50, a first feed device 60, a second feed device 50, and a third feed device 80. Figure 2 shows the first mixing chamber 20 and the first feed device 60 of a device according to a further embodiment. While the first mixing chamber 20 and the first feed device 60 of the device in Figure 2 differ from the embodiment in Figure 1 in a few details, the remaining components (first interaction channel 30, second mixing chamber 40, second interaction channel 50, second feed device 50, and third feed device 80) can be identical to those in Figure 1. Figures 3 to 5 each show a sectional view of the device 1 from Figure 2 along the lines A'-A", B'-B", and C'-C", respectively. In the following, the embodiments of Figures 1 and 2 are described together due to their many similarities. Differences will be discussed where appropriate.

The first mixing chamber 20 has a first inlet opening 201, a second inlet opening 202, and an outlet opening 203. A first fluid Fi can be introduced into the first mixing chamber 20 via the first inlet opening 201, and a second fluid F ₂ can be introduced via the second inlet opening 202. In the first mixing chamber 20, the first and second fluids Fi, F ₂ form an intermediate fluid mixture F12, which can be discharged via the outlet opening 203 of the first mixing chamber 20.

The first supply device 60 is connected (fluidically) to the first mixing chamber 20 via the first inlet opening 201 and serves to introduce the first fluid Fi into the first mixing chamber 20. The second supply device 70 is connected (fluidically) to the first mixing chamber 20 via the second inlet opening 202 and serves to introduce the second fluid F ₂ into the first mixing chamber 20.

The first interaction channel 30 is connected downstream of the outlet opening 203. This channel has an inlet opening 301 and an outlet opening 302. The inlet opening 301 of the first interaction channel 30 coincides with the outlet opening 203 of the first mixing chamber 20, so that the intermediate fluid mixture F12 can flow from the first mixing chamber 20 into the first interaction channel 30.

The second mixing chamber 40 has a first inlet opening 401, a second inlet opening 402, and an outlet opening 402. The first inlet opening 401 coincides with the outlet opening 302 of the first interaction channel 30. The intermediate fluid mixture F12 can be introduced into the second mixing chamber 40 via the first inlet opening 401, and a third fluid F3 can be introduced via the second inlet opening 402. In the second mixing chamber 40, the intermediate fluid mixture F12 and the third fluid F3 form the fluid mixture F123, which can be discharged via the outlet opening 403 of the second mixing chamber 40.

The second interaction channel 50 is connected downstream of the outlet opening 402. This channel has an inlet opening 501 and an outlet opening 502. The inlet opening 501 of the second interaction channel 50 coincides with the outlet opening 403 of the second mixing chamber 40. The generated fluid mixture F123 can be removed from the device 1 via the outlet opening 502. According to one embodiment, the device 1 does not have a second interaction channel, and the generated fluid mixture F123 can be removed from the device 1 via the outlet opening 403 of the second mixing chamber 40.

The first supply device 60 comprises a fluidic component 10 with two bypass channels (feedback channels) 104a, 104b as a means for generating a spatially and/or temporally mobile first fluid Fi and, in particular, for generating a spatial oscillation of the first fluid Fi. The fluidic component 10 shown in Figure 1 with the bypass channels 104a, 104b is merely exemplary. In principle, other fluidic components can also be used, such as so-called feedback-free components.

The energy for generating the spatially and/or temporally mobile fluid jet results from the inlet pressure (at the inlet opening of the flow chamber 100) of the first fluid Fi (also referred to as the first phase A). The inlet pressure can assume values of up to 1000 bar. Typically, the inlet pressure is below 400 bar. Preferably, the inlet pressure is between 0.5 and 200 bar, particularly preferably between 1 and 25 bar. For applications for the generation of liquid nanoparticles, these are generally below 10 bar. The use of the fluidic component 10 has the advantage that This eliminates the need for an additional energy source, reducing the complexity and error-proneness of the device. It also ensures that no additional external energy is introduced into the fluids. The introduction of additional/external energy can destroy sensitive components of the fluids (e.g., long-chain molecules) and should therefore be avoided.

The fluidic component 10 comprises a flow chamber 100 through which a first fluid (stream) Fi can flow. The fluidic component 10 has the function of inducing an oscillation of the first fluid Fi, so that the first fluid Fi oscillates temporally and/or spatially upon entering the first mixing chamber 20 through the first inlet opening 201 of the mixing chamber 20. The temporal frequency of the oscillation is typically 1 Hz to 10 kHz, preferably 10 Hz to 10 kHz, and particularly preferably 100 Hz to 5 kHz.

The flow chamber 100 comprises an inlet opening 101 with an inlet width bioi, through which the first fluid flow Fi enters the flow chamber 100, and an outlet opening 102 with an outlet width b 2, through which the first fluid flow Fi exits the flow chamber 100. The inlet opening 101 and the outlet opening 102 are each defined where the cross-sectional area (transverse to the fluid flow direction) of the fluidic component 10, which the fluid flow passes through when it enters the flow chamber 100 or exits the flow chamber 100, is the smallest. The widths bi and b 2 of the inlet and outlet openings 101, 102, respectively, correspond to the extent of the inlet and outlet openings 101, 102, respectively, transverse to the fluid flow direction and within the oscillation plane of the first fluid Fi (explained later).

The outlet opening 102 of the flow chamber 100 of the fluidic component 10 corresponds here to the first inlet opening 201 of the first mixing chamber 20.

The inlet width bi can range from 0.15 pm to 5,000 pm. The minimum dimensions of the narrowest cross-sectional areas within the fluidic component 10 can be selected depending on the desired volume flow. The higher the volume flow at a constant inlet pressure (at the inlet opening 101 of the flow chamber 100), the larger the dimensions, e.g., of the inlet width bi oi and/or the inlet height hi, must be. Typical dimensions range from 100 pm to 1,500 pm. Typical values for the width bi are 100 pm, 150 pm, 300 pm, 600 pm, and 1,200 pm. The inlet opening 101 and the outlet opening 102 are arranged on two fluidically opposite sides of the fluidic component 10. The flow chamber 100, more precisely a main flow channel 103 of the flow chamber 100, connects the inlet opening 101 and the outlet opening 102 in a non-obstruction-free manner. In an embodiment not shown, the inlet opening 101 and the outlet opening 102 can be connected by means of a non-obstruction-free flow chamber.

The first fluid flow Fi moves in the flow chamber 100 essentially along a longitudinal axis A of the fluidic component 1 (which connects the inlet opening 101 and the outlet opening 102) from the inlet opening 101 to the outlet opening 102. The longitudinal axis A forms an axis of symmetry of the fluidic component 1. The longitudinal axis A lies in two mutually perpendicular planes of symmetry S1 and S2, with respect to which the fluidic component 1 is mirror-symmetrical.

For targeted fluid flow direction changes, the flow chamber 100 comprises two secondary flow channels 104a, 104b in addition to the main flow channel 103. The main flow channel 103 and the two secondary flow channels 104a, 104b extend substantially along the longitudinal axis A of the fluidic component 10, with the main flow channel 103 (viewed transversely to the longitudinal axis A) being arranged between the two secondary flow channels 104a, 104b. Immediately behind the inlet opening 101, the flow chamber 100 divides into the main flow channel 103 and the two secondary flow channels 104a, 104b, which rejoin immediately before the outlet opening 102. In the embodiment illustrated here, the two secondary flow channels 104a, 104b are arranged symmetrically with respect to the plane of symmetry S2 (Figure 4). These secondary flow channels can also be arranged outside the illustrated flow plane. These channels can be realized, for example, by pipes that are also located outside the plane of symmetry S1 or by channels that are at an angle to the flow plane (plane of symmetry S1).

The main flow channel 103 connects the inlet opening 101 and the outlet opening 102 to one another in a substantially straight line, so that the fluid flow Fi flows substantially along the longitudinal axis A of the fluidic component 10. Starting from the inlet opening 101, the secondary flow channels 104a, 104b each extend in a first section at an angle of substantially 90° to the longitudinal axis A in opposite directions. Subsequently, the secondary flow channels 104a, 104b bend so that they each extend substantially parallel to the longitudinal axis A (in the direction of the outlet opening 102) (second section). In order to rejoin the secondary flow channels 104a, 104b and the main flow channel 103, the secondary flow channels 104a, 104b change their direction again at the end of the second section so that they are each directed substantially toward the longitudinal axis A (third section). In the embodiments of Figures 1 and 2, the direction of the secondary flow channels 104a, 104b changes by an angle of approximately 120° at the transition from the second to the third section. However, for the change of direction between these two sections of the secondary flow channels 104a, 104b, angles other than the one mentioned here can be selected or even follow a completely different course.

The bypass channels 104a, 104b are a means for influencing the direction of the first fluid flow Fi flowing through the flow chamber 100. For this purpose, the bypass channels 104a, 104b each have an inlet 104a1, 104b1, formed by the end of the bypass channels 104a, 104b facing the outlet opening 102, and an outlet 104a3, 104b3, formed by the end of the bypass channels 104a, 104b facing the inlet opening 101. A small portion of the first fluid flow Fi, the bypass flows, flows through the inlets 104a1, 104b1 into the bypass channels 104a, 104b. The remaining portion of the first fluid flow Fi (the so-called main flow) exits the fluidic component 10 via the outlet opening 102. The secondary flows exit the secondary flow channels 104a, 104b at the outlets 104a3, 104b3, where they can exert a lateral (transverse to the longitudinal axis A) impulse on the first fluid flow Fi entering through the inlet opening 101. The direction of the first fluid flow Fi is influenced such that the main flow exiting the outlet opening 102 spatially oscillates, specifically in a plane in which the main flow channel 103 and the secondary flow channels 104a, 104b are arranged. The plane in which the main flow oscillates is also referred to as the oscillation plane and essentially corresponds to the plane of symmetry S1 or is parallel to the plane of symmetry S1 (Figure 3).

In the embodiment shown here, the secondary flow channels 104a, 104b each have a cross-sectional area which, over the entire length (from the inlet 104a1, 104b1 to the outlet 104a2, 104b2) of the secondary flow channels 104a, 104b, is almost is constant. In contrast, the size of the cross-sectional area of the main flow channel 103 increases substantially continuously in the flow direction of the main flow (i.e., in the direction from the inlet opening 101 to the outlet opening 102) (Figures 1 and 2). In both embodiments, the shape of the main flow channel 103 is, for example, mirror-symmetrical to the planes of symmetry S1 and S2.

However, the cross-sectional area of the main flow channel 103 can in principle also decrease downstream.

The main flow channel 103 is separated from each secondary flow channel 104a, 104b by a block 11a, 11b. In the embodiments of Figures 1 and 2, the two blocks 11a, 11b are arranged symmetrically with respect to the mirror plane S2. In principle, however, they can also be designed differently and not aligned symmetrically. If the alignment is not symmetrical, the shape of the main flow channel 103 is also not symmetrical with respect to the mirror plane S2. A symmetrical embodiment of the two blocks 11a, 11b is preferred.

The shapes of blocks 11a, 11b shown in Figures 1 and 2 are only examples and can be varied. Blocks 11a, 11b have rounded edges. Sharp edges are also possible. The design variant with rounded edges is preferred. Blocks 11a, 11b in Figures 1 and 2 differ in the shape of their side facing the main flow channel 103. While in Figure 1 this side is almost flat, in Figure 2 it has a curvature.

Upstream of the inlet opening 101 of the flow chamber 100 is a funnel-shaped extension 106, which tapers towards the inlet opening 101 (downstream). In principle, an extension 106 is also possible that has a substantially constant cross-section or, in sections, an expanded cross-sectional area. This funnel-shaped extension can also be referred to as an inlet channel. The flow chamber 100 also tapers, specifically in the region of the outlet opening 102 downstream of the inner blocks 11a, 11b. The taper is formed by an outlet channel 107 and begins at the bypass channel inlet 104a1, 104b1. The extension 106 and the outlet channel 107 taper in such a way that only their width, i.e. their extent in the symmetry plane S1 perpendicular to the longitudinal axis A, decreases downstream. In this embodiment, the taper does not affect the depth (i.e. the extent in the symmetry plane S2 perpendicular to the longitudinal axis A) of the extension 106 and the outlet channel 107 (Figure 3). Alternatively, the Extension 106 and outlet channel 107 also taper in width and depth, respectively. Furthermore, only extension 106 can taper in depth or width, while outlet channel 107 tapers in both width and depth, and vice versa. The shape of extension 106 and outlet channel 107 are shown in Figures 1 and 2 only as examples. Here, their width decreases linearly downstream, with the boundary walls of the extension 106 and the outlet channel 107 (each viewed in the oscillation plane) enclosing an angle E and (p) respectively. Other forms of tapering are possible. The length hoe of the inlet channel of the funnel-shaped extension 106 corresponds, for example, to at least 1.5 times the inlet width bioi, so hoe ≤ 1.5xb i. According to a preferred embodiment, the length hoe of the funnel-shaped extension 106 is greater than 7.5 times the width bioi. For a given and fixed value of the width bi, the following applies: the smaller the angle £, the longer the inlet channel 106 should be.

The inlet opening 101 and the outlet opening 102 each have an idealized rectangular cross-sectional area. These each have the same depth (extension in the plane of symmetry S2 perpendicular to the longitudinal axis A, Figure 3), but differ in their width b1i, b2 (extension in the plane of symmetry S1 perpendicular to the longitudinal axis A, Figure 2). In principle, the corners of the cross-sectional areas can be rounded, and the opposing surfaces that define the inlet and outlet openings 101 and 102, respectively, do not have to be parallel.

The outlet opening 102 of the flow chamber 100 of the fluidic component 10 corresponds in Figures 1 and 2 to the first inlet opening 201 of the first mixing chamber 20. At the outlet opening 102 and the first inlet opening 201 (which are identical in shape and size), respectively, the tapered outlet channel 107 of the fluidic component 10 and the later-explained, widening inlet channel 206 of the first mixing chamber 20 meet, so that an edge is formed in this transition region. This transition region can preferably be rounded. The rounding can have a radius 109 that is smaller than the minimum width of bi (width of the inlet opening 101) and bn (corresponding width of the smallest cross-sectional area An in the main flow channel 103 between the inner blocks 11a, 11b, Figure 2). An extreme value, which results in a sharp-edged outlet 102, is a radius of zero. Due to its greater mechanical stability, a radius of 109 is preferable. The widths bioi, bn, and b2 are approximately equal. For example, they can be approximately 0.3 mm. The radius 109 at the outlet opening 102 can then be approximately 0.025 mm. Downstream of the first inlet opening 201 of the first mixing chamber 20 is an inlet channel 206. The inlet channel 206 has a cross-sectional area that increases downstream (transverse to the first fluid flow direction or to the longitudinal axis L of the first mixing chamber 20). In particular, the width (extension in the oscillation plane and transverse to the longitudinal axis L) of the inlet channel 206 increases downstream. The width increases linearly here. However, the increase in width can also follow a polynomial. The walls delimiting the inlet channel 206 enclose an angle θ when viewed in the oscillation plane. This angle θ can have different dimensions. An angle θ that is selected depending on the oscillation angle α is advantageous. A deviation from the oscillation angle α of +40° and -10° is possible, i.e. α - 10° < θ < α + 40°. A particularly preferred value for the angle θ is α - 5° < θ < α + 20°. The oscillation angle α here corresponds to the natural oscillation angle of the oscillating first fluid Fi, which would occur in the absence of the inlet channel 206 and the first mixing chamber 20. In the embodiments of Figures 1 and 2, the angle θ is different. The first inlet opening 201 is thus defined in the inlet channel 206 where it has the smallest cross-sectional area (transverse to the first fluid flow direction Ri) or the smallest width (parallel to the oscillation plane and transverse to the first fluid flow direction Ri).

The width b2o of the first mixing chamber 20 is defined by two approximately parallel and flat surfaces that function as boundary walls in an intermediate section of the first mixing chamber 20. The intermediate section is formed along the first fluid flow direction Ri between the inlet channel 206 and an outlet channel 207 of the first mixing chamber 20. In principle, the boundary walls can also be designed differently (other than flat and parallel).

The outlet channel 207 adjoins the downstream end of the intermediate section. Its cross-sectional area (transverse to the first fluid flow direction or to the longitudinal axis L of the mixing chamber 20) decreases downstream along the longitudinal axis L. In particular, the width (extension in the oscillation plane and transverse to the longitudinal axis L) of the outlet channel 207 decreases downstream. The width decreases linearly here. However, the decrease in width can also follow a polynomial. The walls delimiting the outlet channel 207 enclose an angle w when viewed in the oscillation plane. In the embodiments of Figures 1 and 2, the angle w is different. The downstream end of the outlet channel 207 is formed by the outlet opening 203. The outlet opening 203 is thus defined in the outlet channel 207 where it has the smallest cross-sectional area (transverse to the fluid mixture flow direction R12) or the smallest width (parallel to the oscillation plane and transverse to the fluid mixture flow direction R12). The intermediate fluid mixture F12 consisting of the first and second fluids F1, F2 leaves the first mixing chamber 20 through its outlet opening 203.

If the first mixing chamber 20 merges into the first interaction channel 30 without a change in cross-section, the length I20 of the first mixing chamber 20 is defined as a function of 20 times the diameter D202 of the second inlet opening 202 of the first mixing chamber 20. Therefore, I20 ~ 20XD202 applies.

The outlet opening 203 has a cross-sectional area A203, which is, for example, rectangular and therefore has a width b203 and a height _h2os . In principle, a non-rectangular cross-sectional area of the outlet opening 203 is also possible. The cross-sectional area A203 is larger than the smallest cross-sectional area of the fluidic component 10 (A101, An, or A102). The cross-sectional area A203 is equal to or larger than the sum of the cross-sectional area A202 of the second inlet opening 202 of the first mixing chamber 20 and the smallest cross-sectional area of the fluidic component 10 (A101, An, or A102).

The outlet channel 207 has the fluidic effect of contracting the vortices generated by the Fulda component 10 to a smaller cross-section. Since the circulation present in a vortex must be maintained according to Helmholtz's vortex laws, the contraction of the vortices leads to an increase in the vortex velocity and thus to an increase in the transverse velocities in the fluid. The higher velocities lead to faster mixing of the fluids and also to faster decay of the vortices, which in turn leads to better mixing on the smaller scales. This vortex decay essentially determines the length I30 of the first interaction channel 30, which adjoins the first flow chamber 20. The outlet channel 207 of the first mixing chamber 20 thus contributes significantly to the rapid mixing of the fluids F1, F2. In order to utilize this effect, the ratio of the maximum cross-sectional area A20 of the first mixing chamber 20 (where A20 = b20 x h20, see Figures 2 and 3) to the cross-sectional area A203 of the outlet opening 203 (where A203 = b203 xh ₂ 03, see Figures 2 and 3) must be selected such that 2 < A20/A203 < 100, preferably 2 < A20/A203 < 50 and particularly preferably 3 < A20/A203 < 20. In an embodiment not shown, several outlet openings 203 can also be provided, which open into parallel-connected interaction channels 30 and then into parallel-connected second mixing chambers. The sum of the cross-sectional areas A203 of the individual outlet openings 203 is greater than the smallest cross-sectional area of the fluidic component 10 (A101, A102, or A103).

The second inlet opening 202 is formed in the inlet channel 206. Alternatively, the second inlet opening 202 can be formed in the outlet channel 207. It is conceivable that more than one second inlet opening (for introducing the second fluid F2 or other fluids) is provided. Preferably, at least one of the second inlet openings 202 is located in the inlet channel 206.

In Figures 1 and 2, the second inlet opening 20 is circular, but a non-circular shape of the second inlet opening 202 is also possible. The cross-sectional area of the second inlet opening 202 is approximately the same size as the cross-sectional area of the first inlet opening 201.

The distance of the second inlet opening 202 from the first inlet opening 201 along the first fluid flow direction Ri is shown in Figure 2 as I202. It is advantageous if the length I202 corresponds at least to the width b2oi of the first inlet opening 201 (or outlet opening 102), i.e., I202 s b2oi. It is particularly advantageous if the length I202 corresponds at least to the sum of the width b2oi and the width b2oi of the first and second inlet openings 201, 202 or at least twice the width of b2oi, i.e., I202 s (b2oi + b202) or I202 s 2 x b2oi.

Figure 3 shows a sectional view of the device 1 from Figure 2 along the line A'-A" (perpendicular to the sectional plane in Figure 2). Accordingly, in this embodiment, the fluidic component 10, the first mixing chamber 20 and at least the upstream end of the first interaction channel 30 have a constant height h. The height (also called depth) is the extent transverse to the oscillation plane of the first fluid Fi . In an embodiment not shown, the height h may not be constant. In particular, in the region of the inlet channels 106 and 206 and the outlet channels 107 and 207, the height h may deviate from the height in the rest of the device.

Figure 3 shows that the second feed device 70 opens into the second inlet opening 202 of the first mixing chamber 20. The second feed device 70, which is used to introduce of the second fluid F2 into the first mixing chamber 20, comprises a supply channel 701 which extends along a longitudinal axis and predetermines the fluid flow direction R ₂ for the second fluid F ₂ (Figure 3). The supply channel 701 is connected to the first mixing chamber 20 via the second inlet opening 202 of the first mixing chamber 20. The supply channel 701 is (as viewed in the plane of symmetry S2 or a plane which runs perpendicular to the oscillation plane and along the longitudinal axis L) at an angle ß to the oscillation plane of the fluidic component 10 or the plane of symmetry S1. In this embodiment, the angle ß = 90°. In principle, the angle can assume a different value. The angle ß influences the mixing quality and/or the mixing path length or the mixing time.

Figure 4 shows a sectional view of the device 1 from Figure 2 along the line B'-B". In this sectional view, the cross-sectional area of the main flow channel 103 and the secondary flow channels 104a, 104b of the fluidic component 10 can be seen. In this embodiment, the heights hios, hi ₀ 4a, hi ₀ 4b of the channels 103, 104a, 104b are the same. However, they can in principle also differ from one another. In Figure 4, the cross-sectional areas of the main and secondary flow channels 103, 104a, 104b are shown in a simplified manner with sharp edges. However, the corners can be provided with radii, i.e., rounded.

Figure 5 shows a sectional view of the device 1 from Figure 2 along the line O-C". In this sectional view, a cross-section through the inlet channel 206 of the first mixing chamber 20 can be seen. Again, for simplicity, the corners are not shown with radii, although these may be present. The distance between the lateral boundary walls of the inlet channel 206 (parallel to the oscillation plane and transverse to the longitudinal axis L) is constant over the entire height h ₂₀ 6 . However, this distance can also change along the height h ₂₀ 6 .

Figure 5 also shows that the second inlet opening 202 of the first mixing chamber 20 is formed in its inlet channel 206. Viewed in a plane transverse to the longitudinal axis L, the supply channel 701 forms an angle q with the oscillation plane. In the illustrated embodiment, the angle q = 90°. In principle, the angle can assume a different value, e.g., between 30° and 150°. An angle q of 90° is preferred. The mixing of the first and second fluids Fi, F2 in the first mixing chamber 20 is characterized by the fact that the fluidic component 10 generates strong velocity fluctuations transverse to the main flow direction of the first fluid flow direction Ri (i.e. essentially in the Y direction (Figure 1 )), which lead to a rapid mixing of the two fluid flows by chaotic advection.

Furthermore, the fluidic component 10 creates large-scale vortices, which successively break down into smaller vortices through fluid-mechanical processes and are finally dissipated by viscous processes. This cascade of vortices, in addition to the dissipation of the vortices, leads to a mixing of the fluids F1 and F2 on increasingly smaller scales. This mixing takes place (mostly) in the first mixing chamber 20.

The first interaction channel 30 is connected to the outlet opening 203 of the first mixing chamber 20. In the first interaction channel 30, mixing continues continuously until, after a characteristic mixing time tmix, a sufficiently homogeneous mixture of the two fluids F1, F2 is obtained. This mixing time tmix can be in the range from 0.1 ms to 1000 ms (0.1 ms to 1 ms, 1 ms to 1000 ms). Typically, the mixing time tmix is between 0.1 ms and 500 ms (1 ms to 500 ms) and in particular between 0.1 ms and 100 ms (1 ms to 100 ms). Mixing should be completed in the first interaction channel 30. For this purpose, the length I20 of the first mixing chamber 20 and the length I30 of the first interaction channel 30 can be selected to be so large that a particle transported at the average speed can completely pass through the first mixing chamber 20 and the first interaction channel 30 within the mixing time tmix.

In Figure 1, the first interaction channel 30, starting from its inlet opening 301, initially has a section with a constant cross-sectional area. Downstream is a section in which the cross-sectional area increases downstream. This section is symmetrical with respect to the fluid mixture flow direction R12. This is followed downstream by another section with a constant cross-sectional area, which in turn is followed by a section in which the cross-sectional area increases downstream. This section is asymmetrical with respect to the fluid mixture flow direction R12.

The first interaction channel 30 can widen one or more times (increase in the cross-sectional area, in particular increase in the width transverse to the fluid mixture flow direction Ri2 and parallel to the oscillation plane). It is also possible for the first interaction channel 30 to taper one or more times (decrease in cross-sectional area, in particular increase in width transverse to the fluid mixture flow direction R12 and parallel to the oscillation plane). By changing the cross-sectional area _A30 of the first interaction channel 30 along the fluid mixture flow direction R12 in this way, an improvement in the mixing of pulsating flows can be achieved at low Reynolds numbers (<10), and at significantly higher Reynolds numbers (<100), pulsations in the mixing caused by the fluidic component 10 can be reduced. The cross-sectional changes are within a range that prevents separation (so-called dead water areas), which could lead to indefinite residence times of the intermediate fluid mixture in the first interaction channel 30. This is achieved by ensuring that the angle A30 is less than 10°. This angle is defined between the center line of the interaction channel 30 and the bounding wall of the interaction channel 30 in a widening section (viewed in the fluid mixture flow direction R12). If the first interaction channel 30 widens several times (viewed in the fluid mixture flow direction R12), there are multiple angles A30, for example, the upstream angles _A30 and _A30ib and the downstream angle _A30OÜ in Figure 1. Preferably, the angle A30 is less than 8°. Advantageously, the angle A30 is between 2° and 6°. In the illustrated embodiment, an upstream symmetrical widening is realized in the interaction channel 30, in which the angles _A30 and _A30ib are equal.

In Figure 1, the interaction channel 30 is designed to be rectilinear (extending along the fluid mixture flow direction R12). In principle, it can also be non-reciprocal and, for example, have at least one meandering section, as shown by way of example in Figure 6. Depending on the fluids Fi, F2 to be mixed, such meanders can extend the residence time in the interaction channel 30 and thus enable secondary mixing. This is advantageous for certain intermediate fluid mixtures F12 consisting of the fluids Fi, F2, which require a certain maturation time and thus have a longer mixing time tmix.

In order to stop the growth of the particles after the mixing time tmix and to further stabilize the particles, the intermediate fluid mixture F12 (with the particles) is combined with the third fluid F3 in the second mixing chamber 40. For this purpose, the intermediate fluid mixture F12 enters the second mixing chamber 40 from the first interaction channel 30 via the first inlet opening 401 and the third fluid F3 via the second inlet opening 402. The third fluid F3 flows from a supply channel 801 of the third Feed device 80. When mixing the intermediate fluid mixture F12 and the third fluid F3 in the second mixing chamber 40, the particles are exposed to as little mechanical stress as possible to prevent damage to the particles, as well as fusion and sticking (agglomeration and aggregation) of the particles. For this purpose, the magnitude and direction of the stress are very similar to those of the intermediate fluid mixture F12 and the third fluid F3.

The claimed method for generating a fluid mixture may require that the intermediate fluid mixture F12 has an average velocity U302 at the outlet opening 302 of the first interaction channel 30, the third fluid _F3 has an average velocity U402 at the second inlet opening 402 of the second mixing chamber 40, and the fluid mixture F123 has an average velocity U403 at the outlet opening 403 of the second mixing chamber 40, wherein the ratio of the velocities is 0.8 < U402/U302 < 1.2 and 0.8 < U403/U302 < 1.2. The desired velocity ratio can be adjusted by the size of the cross-sectional areas of the outlet openings 302, 403 and the second inlet opening 402, taking into account the volume flows of the intermediate fluid mixture F12 and the third fluid F3. If the volume flow of the intermediate fluid mixture F12 is twice the volume flow of the third fluid _F3 , the cross-sectional area of the outlet opening 302 must be selected to be twice the cross-sectional area of the second inlet opening 402 ( _A3 o2 = _2A4 o2), and the cross-sectional area of the outlet opening 403 must be three times the cross-sectional area of the second inlet opening 402 ( _A4 o3 = _3A4 o2). If the outlet openings 302, 403 and the second inlet opening 402 have the same height, the ratio of the cross-sectional areas is transferred to the corresponding widths.

In summary, the cross-sectional area of the outlet opening A403 of the second mixing chamber 40 approximately corresponds to the sum of the cross-sectional area of the outlet opening A302 (the first inlet opening A401) and the cross-sectional area of the second inlet opening A402. This is particularly the case when the direction R3 of the third fluid F3 and the direction R12 of the intermediate fluid mixture F12 are within the oscillation plane or parallel to the oscillation plane.

The transition from the first interaction channel 30 to the second mixing chamber 40 (i.e., the position of the outlet opening 302 of the first interaction channel 30 and the first inlet opening 401 of the second mixing chamber 40) is characterized by a sudden increase in the cross-sectional area (transverse to the fluid mixture flow direction R12). In the area of this sudden increase in cross-section, a Feed channel 801 of the third feed device 80 into the second mixing chamber 40. The feed channel 801 extends (rectilinearly) along the third fluid flow direction R ₃ . The third fluid flow direction R ₃ and the fluid mixture flow direction R 12 enclose an angle £ that is less than or equal to 90°, preferably less than 45°, particularly preferably between 5° and 40°.

The generated fluid mixture FI ₂₃ flows from the outlet opening 403 of the second mixing chamber 40 into the second interaction channel 50 and leaves the device 1 through the outlet opening 502 of the second interaction channel 50.

Figure 6 shows a device 1 according to a further embodiment. This differs from the embodiments of Figures 1 to 5 particularly in the shape of the first interaction channel 30. Thus, the first interaction channel 30 has a meandering section with (here, by way of example) a 180° deflection 303 and two 90° deflections 304. The meandering section extends the first interaction channel 30, so that the residence time of the intermediate fluid mixture F12 in the first interaction channel 30 is extended (compared to the embodiment of Figure 1).

In this embodiment, the interaction channel 30 has a constant channel width b ₃ oo in the deflections 303, 304.

Immediately downstream of the last deflection 304, the meandering section is followed by a straight-line section 305. The straight-line section 305 has a length l ₃ os that is at least three times the channel width b ₃ oo (l 3 0 5 x b ₃ oo), preferably at least five times the channel width b ₃ oo (l 3 0 5 x b ₃ oo). The straight-line section 305 serves to even out the velocity profile of the intermediate fluid mixture F12.

Downstream of the straight-line section 305 is an asymmetric section 307. The asymmetric section 307 accommodates the asymmetric flow velocity profile of the intermediate fluid mixture F12. The asymmetric section 307 prevents the formation of recirculation regions. This widening is achieved by the angle A ₃ o.

Immediately downstream of the asymmetric section 307, another straight-shaped section 308 is arranged. The length l ₃ os of this section depends on the desired mixing time tmix of the fluids Fi, F ₂ to be mixed in order to produce particles with the desired Size and shape. Mixing times of around 10 ms are required to produce lipid nanoparticles.

In this embodiment, the cross-sectional area A201 of the first inlet opening 201 of the first mixing chamber 20 is approximately 25% larger than the cross-sectional area A202 of the second inlet opening 202 of the first mixing chamber 20.

An embodiment is also conceivable which differs from that of Figure 6 in that the first interaction channel 30 does not comprise the deflections 303 and 304, but only the rectilinear section 305 (which directly adjoins the first mixing chamber 20), a widening symmetrical section 307 and the rectilinear section 308.

The second interaction channel 50 extends (generally) along an axis corresponding to the direction of the fluid mixture F123. The direction of the fluid mixture F123 results from the velocity vector of the fluid mixture F123. The velocity vector of the fluid mixture F123 corresponds to the sum of the velocity vector of the intermediate fluid mixture F12 at the first inlet opening 401 and the velocity vector of the third fluid F3 at the second inlet opening 402. The axis of the second interaction channel 50 and the fluid mixture flow direction R12 enclose an angle e, which in the embodiment of Figure 6 is less than 180°. The axis of the second interaction channel 50 and the third fluid flow direction R3 enclose an angle K, which in the embodiment of Figure 6 is less than 180°. The angles e and K are different sizes here, in particular, the angle K is greater than the angle e. For example, the angle K is between 170° and 179° (174°) and the angle e is between 160° and 169° (166°). The angle between the fluid mixture flow direction R12 and the third fluid flow direction R3 and the angles e and K add up to 360°.

Figure 7 schematically illustrates the displacement of the moving (oscillating) first fluid Fi (at the outlet opening 102 of the fluidic component 10) over time. Accordingly, the first fluid Fi oscillates periodically between two maximum displacements, for example, approximately +25° and -25°. The dashed line represents an idealized sinusoidal curve. To increase the mixing quality in the first mixing chamber 20, an additional intermediate oscillation is advantageous. The curve shown with a solid line includes such an intermediate oscillation. For example, the intermediate oscillation is provided at approximately ±5°. Such a The temporal progression, as shown by the solid line, can be generated, for example, with the fluidic components 10 according to Figure 1 or 2. The oscillation angle α can be selected depending on the desired mixing quality, the fluids to be mixed, and their volumes. The oscillation angle α can be determined in various ways. For example, from the ratio of the velocity components in the center of the cross-sectional area of the outlet opening 102 according to the relationship a = 2 * arctan (v / u), where u is the velocity component in the flow direction and v is the velocity component perpendicular to the flow direction, in the oscillation plane.

In the first mixing chamber 20, the first fluid Fi preferably has a degree of turbulence TU20 greater than 0.05, particularly preferably the degree of turbulence is between 0.1 and 0.5. In general, the degree of turbulence indicates the variation in speed in relation to the average speed. The degree of turbulence is specifically defined here as the quotient of the maximum temporal fluctuation _ou , _max ,2o of the local speed of Fi in the first mixing chamber 20 and the average speed U201 of the first fluid Fi at the first inlet opening 201: TU20 = a _u ,max,2o / U201 ■ To determine the maximum temporal fluctuation, the temporal variance ou _of the speed is determined with the aid of a transient numerical simulation of the flow (CFD) of the first fluid Fi. The spatial maximum of _ou in the mixing chamber 20 is identified.

In the second mixing chamber 40, the degree of turbulence TU40 is defined according to TU40 = o _u ,max,4o / U401, where o _u ,max,4o is the maximum variance of the velocity of F12 in the mixing chamber 40 and U401 is the velocity of the intermediate fluid mixture F12 at the first inlet opening 401 of the second mixing chamber 40. Preferably, the degree of turbulence TU40 is less than 0.1, more preferably less than 0.05, and especially preferably less than 0.025.

In the first mixing chamber 20 of the embodiments presented here, a Kolmogorov scale Lk (length scale of the smallest vortices in the turbulent flow) of less than 20 pm, preferably less than 10 pm and particularly preferably less than 5 pm, can be achieved, in particular by the respective fluidic component 10 for the rapid mixing of the first and second fluids Fi, F2. The Kolmogorov scale Lk can be estimated from the results of a turbulent CFD (Reynolds Averaged Navier Stokes, RANS for short). For this purpose, the turbulent dissipation rate, e, which is defined as The transport quantity of a so-called k-e turbulence model is calculated and related to the kinematic viscosity v of the fluid mixture F12 as follows:

Lk = ^/ ³ /E .

In contrast to the mixing in the first mixing chamber 20, the mixing in the second mixing chamber 40 should occur with the lowest possible shear of the intermediate fluid mixture F12. For this purpose, the relative differences between the velocities U401 at the first inlet opening 401 of the second mixing chamber 40 (or at the outlet opening 302 of the first interaction channel 30) and U402 at the second inlet opening 402 of the second mixing chamber 40 are as small as possible. In absolute terms, the turbulence in the second mixing chamber 40 should also be lower than in the first mixing chamber 20. For this purpose, the absolute velocities in the second mixing chamber 40 can be lower than in the first mixing chamber 20. Preferably, U401 < U201 , particularly preferably U401 < U201 / 2, where U401 is the velocity of the intermediate fluid mixture F12 at the first inlet opening 401 of the second mixing chamber 40 and U201 is the velocity of the first fluid Fi at the first inlet opening 201 of the first mixing chamber 20.

Figure 8 shows a further embodiment of the device 1. This embodiment differs from those of Figures 1 to 6, in particular in the design of the first supply device 60 and in the number of third supply devices 80a, 80b, 80c, 80d. Thus, the fluidic component 10 of the first supply device 60 has only one secondary flow channel 104. This secondary flow channel 104 is annular and arranged upstream of the main flow channel 103. Four third supply channels 801a, 801b, 801c, 801d open into the second mixing chamber 40.

In Figure 8, the bypass channel 104 has a substantially constant cross-sectional area over its entire length (between points 104a1 and 104b1). In the region of each bypass channel inlet or outlet (at points 104a1 and 104b1), an increase in the respective cross-sectional area is provided. In principle, the size of the cross-sectional area here can also be as large as over the entire length of the bypass channel 104.

At the transition between the secondary flow channel 104 and the main flow channel 103, the fluidic component 10 has a width bn (extension parallel to the oscillation plane and transverse to the first fluid flow direction Ri). Preferably, the inlet width bi is smaller than the width bn. The width of the main flow channel 103 initially increases and then decreases downstream, starting from the transition region to the secondary flow channel 104. Compared to the fluidic components 10 of Figures 1 and 2, this fluidic component 10 generates a higher oscillation frequency at the same inlet pressure PIOIN. A higher oscillation frequency shortens the mixing time of the first fluid Fi and the second fluid F2 in the first mixing chamber 20 and the adjoining first interaction channel 30.

In Figure 8, the length I20 (extension along the first fluid flow direction Ri) of the first mixing chamber 20 is smaller than the length I of the fluidic component 10. It should be noted that in this easier-to-manufacture embodiment, the length I includes the length Iwe. In this case, the length Iw is defined from a point on the outer boundary wall of the bypass channel 104, which is at the maximum distance from the outlet opening 102 along the axis X, to the outlet opening 102. The main flow channel 103 and the bypass channel 104 lie in one plane. According to an alternative, the bypass channel 104 can lie in a plane parallel to the plane of the main flow channel 103. In this case, the length Iw does not include the length Iwe. In this case, the length Iw extends from the inlet opening 101 to the outlet opening 102. It is also conceivable that the length I20 is greater than the length Iw.

The third fluid F3 is fed into the second mixing chamber 40 via a plurality of third supply channels 801a, 801b, 801c, 801d. By way of example, there are four third supply channels 801a, 801b, 801c, 801d in Figure 8. A different number is conceivable. The two third supply channels 801a, 801c arranged further upstream are arranged symmetrically to one another (relative to the second mixing chamber 40), while the two third supply channels 801b, 801d arranged further downstream are not arranged symmetrically to one another (or are offset along the fluid mixture flow direction R12). The supply channels 801a, 801b, 801c, 801d are each part of a third supply device 80a, 80b, 80c, 80d. However, the supply channels 801 a, 801 b, 801 c, 801 d can also be part of a common third supply device and be fed by a common inlet which branches into the individual supply channels 801 a, 801 b, 801 c, 801 d.

The plurality of third supply channels 801 a, 801 b, 801 c, 801 d causes the impulse exerted by the third fluid F ₃ on the intermediate fluid mixture F 12 to be comparatively small (relative to the embodiments of Figures 1 to 6), since the impulse is spatially distributed. The cross-sections are designed so that the average velocities at the inlet and outlet openings are as similar as possible. For example, the average velocity U302 of the intermediate fluid mixture F12 at the outlet opening 302 of the first interaction channel 30 is related to the average velocities U402a and U402c of the third fluid _F3 at the second inlet openings 402a and 402c of the second mixing chamber 40: 0.8 < U402a/ _u302 < 1.2 and 0.8 < U402c/ _u302 < 1.2. The volume flow rates through the second inlet openings 402a and 402c, as well as the volume flow rate of the intermediate fluid mixture F12 through the first inlet opening 401, determine the size of the cross-sectional areas at these openings. If the volume flows through the second inlet openings 402a and 402c are equal and each half as large as the volume flow through the first inlet opening 401, then the cross-sectional areas of the second inlet openings 402a and 402c are equal and each half as large as the cross-sectional area of the first inlet opening 401.

Figure 9 shows a further embodiment of the device 1. This differs from those of Figures 1 to 6 and 8 in particular in the design of the first supply device 60. Thus, the first supply device 60 in Figure 9 has two inlet openings 101a, 101b, but no bypass channel. Upstream of the inlet openings 101a, 101b, a projection 106 is provided which, viewed in the fluid flow direction, divides into two channels 106a and 106b. The channels 106a, 106b open into the inlet openings 101a, 101b. The channels 106a, 106b serve to condition the fluid flow of the first fluid Fi. The shape of the two channels 106a, 106b in Figure 9 is only an example. The downstream end of the channels 106a and 106b, which faces the inlet openings 101a, 101b, is formed by a straight end section. The channels 106a, 106b are arranged mirror-symmetrically with respect to a longitudinal axis of the device 1, as are the inlet openings 101a, 101b. The inlet openings 101a, 101b form the transition between the channels 106a, 106b, on the one hand, and the main flow channel 103, on the other. The downstream, straight end sections of the channels 106a and 106b enclose an angle α. This angle α takes on values between 95° and 175°. The apex of the angle α lies downstream of the inlet openings 101a, 101b. The angle o is measured upstream of the apex. The smaller the angle o, the longer the fluidic component 10 becomes.

The embodiment of Figure 9 also differs from the other embodiments in the design of the first interaction channel 30 and the supply channel 801 of the third supply device 80. Thus, the first interaction channel 30 has a section 307 whose cross-section decreases downstream. The section 307 is located closer at the outlet opening 302 than at the inlet opening 301. Likewise, the feed channel 801 has a section 807 whose cross-section decreases downstream. These cross-sectional changes have the effect of reducing relative velocity fluctuations and making the velocity distribution across the cross-section more uniform. Furthermore, the velocities of the intermediate fluid mixture F12 and the third fluid _F3 can be better controlled upon merging, and thus the mixing conditions can be more precisely defined. This makes it possible to precisely define and thus limit the shear during the mixing of the two fluid streams. In order to reduce the velocity fluctuations of the fluids and to equalize the velocity distribution, the cross-sectional area of the outlet opening 302 can be reduced by a factor of 2 to 100, preferably by a factor of 2 to 20, and particularly preferably by a factor of 2 to 10, compared to the maximum cross-sectional area of the first interaction channel 30. Likewise, the cross-sectional area of the second inlet opening 402 can be reduced by a factor of 2 to 100, preferably by a factor of 2 to 20, and particularly preferably by a factor of 2 to 10, compared to the maximum cross-sectional area of the supply channel 801 of the third supply device 80.

The statements regarding the angles e and K in connection with Figure 6 are also transferable to Figure 9.

The embodiment of the device 1 shown in Figure 10 differs from the embodiment of Figure 1 in particular in the design of the fluidic component 10, the first interaction channel 30 and the relative arrangement of the third supply device 80 to the second mixing chamber 40. The relative arrangement is such that the intermediate fluid mixture F12 and the third fluid _F3 meet at an angle of substantially 90° or that the fluid mixture flow direction R12 and the third fluid flow direction _R3 enclose an angle of substantially 90°. In the devices 1 of the other embodiments, this angle is denoted by £ and is smaller than 90°. In Figure 10, the direction _R3 of the third fluid _F3 does not extend in the oscillation plane or parallel to the oscillation plane.

The first interaction channel 30 is tubular with a constant cross-sectional area and constant width along its extension between the inlet opening 301 and the outlet opening 302. The second mixing chamber 40 is formed by an extension of the first interaction channel 30, with the width remaining unchanged. However, the depth of the second mixing chamber 40 is greater than the depth of the first interaction channel. 30. Specifically, in the embodiment of Figure 10 (see also Figure 11), the depth of the second mixing chamber 40 is twice the depth of the first interaction channel 30. Thus, the first inlet opening 401 of the second mixing chamber 40 has a smaller cross-sectional area (depth) than the outlet opening 403 of the second mixing chamber 40. The ratio of the depth of the first inlet opening 401 to the depth of the outlet opening 403 depends on the ratio of the volume flows of the intermediate fluid mixture F12 and the fluid mixture F123. Preferably, the ratio of the depths tt^i is greater than or equal to the ratio of the volume flow of F123 to the volume flow of F12.

The second mixing chamber 40 has a length (extension along the fluid mixture flow direction R12) and a width (extension transverse to the fluid mixture flow direction R12 and transverse to the third fluid flow direction R3), each of which corresponds to the diameter of the second inlet opening 402 of the second mixing chamber 40. The width of the second mixing chamber 40 corresponds to the width of the first inlet opening 401. The ratio of the width of the second mixing chamber 40 to the diameter of the second inlet opening 402 can range from 1:1 to 2:1. The second inlet opening 402 has, for example, a round cross-sectional area. Alternatively, it can be square or oval.

As Figure 11 shows in conjunction with Figure 10, the depth tso2 of the outlet opening 302 of the first interaction channel 30 is significantly smaller than the depth t403 of the outlet opening 403 of the second mixing chamber 40. The cross-sectional area A302 is formed by the width 0302 at the outlet opening 302 and the depth tso2. The cross-sectional area A403 is formed by the width b403 at the outlet opening 403 and the depth t403. The cross-sectional area A402 of the second inlet opening 402 of the second mixing chamber 40 is formed in this embodiment by the diameter dsoi at the outlet opening 402.

In this embodiment, the cross-sectional area of the second inlet opening 402 is significantly larger than that of the first inlet opening 401 (which corresponds to the outlet opening 302), whereby the average velocity at the second inlet opening 402 is significantly lower than the average velocity at the first inlet opening 401. This results in the fluid-mechanical effect that the momentum of the intermediate fluid mixture F12 (which enters the second mixing chamber 40 via the first inlet opening 401) upon entering the second mixing chamber 40 is significantly larger than the momentum of the third fluid F3 (which enters the second mixing chamber 40 via the second inlet opening 402) upon entering the second mixing chamber 40. Although the Since the intermediate fluid mixture F12 and the third fluid F3 meet essentially at a right angle, the different momenta result in only minimal shear of the intermediate fluid mixture F12.

In summary, the cross-sectional area of the outlet opening A403 is smaller than the sum of the cross-sectional area A302 at the outlet opening 302 and the cross-sectional area A402 at the second inlet opening 402. This is the case when the direction R3 of the third fluid F3 is at an angle to the direction R12 of the intermediate fluid mixture F12 and is not within the oscillation plane. In the embodiment shown in Figures 10 and 11, the direction _R3 is orthogonal to the oscillation plane.

In contrast to the embodiment variant in which the direction R3 lies within the oscillation plane, in the embodiment of Figures 10 and 11, the cross-sectional area A403 should be larger than the cross-sectional area A401 (A403 > A401). The following area relationship is preferred: 1.1 A403 < A401 + A402 < 10 A403. The following area relationship is particularly preferred: 1.9 A403 < A401 + A402 < 7.9 A403.

A further feature of the embodiment shown in Figures 10 and 11 is the sudden expansion of the cross-sectional area (transverse to the fluid mixture flow direction R12) at the first inlet opening 401. According to the embodiment shown in section D'-D" in Figure 11, the expansion of the cross-sectional area is step-like. The step is pronounced in the direction of the feed channel 801. The inflow of the third fluid _F3 into the mixing chamber 40 takes place downstream of the step, viewed in the fluid mixture flow direction R12 of the intermediate fluid mixture F12. According to fluid mechanics expertise, such steps should be avoided, as they lead to the formation of recirculation regions (dead water regions), which lead to indefinite residence times of the fluid mixture F123 in the mixing chamber 40 and thus impair its function. In the embodiment shown in Figure 10, the mixing chamber 40 or the ratio of the depth t403 at the outlet opening 403 to However, the depth tso2 at the outlet opening 302 is designed such that the potential recirculation area is only flowed through by the third fluid F3. As a result, only the third fluid F3 is recirculated, for which the residence time in the mixing chamber 40 is irrelevant. The ratio of the depth t403 at the outlet opening 403 to the depth tso2 at the outlet opening 302 depends on the velocity ratio of the fluid F12 and the fluid _F3 . In the embodiment shown in Figures 10 and 11, the depth t403 = 1.8 tso2 with a constant width of bso2 = b403- The embodiment of Figures 10 and 11 combines fluid mechanics aspects for a gentle mixing of the intermediate fluid mixture F12 and the third fluid F3 with a minimalist design.

Figure 12 shows a further embodiment. This differs from that of Figures 10 and 11 particularly in the design of the first interaction channel 30 and the second mixing chamber 40.

The second mixing chamber 40 is tubular with a bend. Specifically, the bend here is L-shaped with two sections arranged at a 90° angle to each other, each of which opens into an open end. The end of the first section of the tubular mixing chamber 40 forms the second inlet opening 402, through which the third fluid F3 enters the mixing chamber 40. The end of the second section of the tubular mixing chamber 40 forms the outlet opening 403, through which the fluid mixture F123 exits the mixing chamber 40.

The first interaction channel 30 is also tubular and has a smaller diameter than the second mixing chamber 40. The tubular interaction channel 30 and the second section of the tubular mixing chamber 40 are arranged concentrically and extend along an axis on which the outlet opening 403 also lies. The first interaction channel 30 protrudes into the mixing chamber 40 in the region of the bend. For this purpose, an opening is provided in the wall of the mixing chamber 40, which corresponds in shape and size to the cross-sectional area of the interaction channel 30. The outlet opening 302 of the first interaction channel 30, which is simultaneously the first inlet opening 401 of the mixing chamber 40, is located upstream of the outlet opening 403. The intermediate fluid mixture F12 enters the mixing chamber 40 via the first inlet opening 401.

In the mixing chamber 40, the intermediate fluid mixture F12 flows in a round jet with the average velocity U302 and the third fluid _F3 flows over the concentric annular gap with the average velocity U401 at the level of the first inlet opening 401. The ratio of the velocities is 0.5 < U401/U302 < 2. The velocities are adjusted via the diameter/cross-sectional areas of the tubes (which form the first interaction channel 30 and the second mixing chamber 40) so that the desired velocity ratios are achieved for the volume flow required for the process. For example, if the volume flows of the third fluid F3 and the intermediate fluid mixture F12 are to be If the particles are to be mixed in a ratio of 3:1 and the cross-sectional areas of the pipes forming the first interaction channel 30 and the second mixing chamber 40 are circular, a ratio of the diameter of the outer pipe to the inner pipe of 2:1 is selected so that an area ratio of 3:1 from the annular gap to the inner pipe results.

Figure 13 schematically shows the sequence of a method for continuously mixing multiple (three or more) fluids to produce a fluid mixture according to one embodiment. Steps shown in dashed or dotted lines represent merely optional process steps.

The process is characterized by the fact that different mixing techniques are combined at very short intervals using a device 1 according to the invention. This achieves high reproducibility and minimizes the risk of errors, thus ensuring consistent quality of the produced fluid mixture and reducing costs.

In the first mixing chamber 20, a rapid/turbulent mixing (degree of turbulence greater than 0.1) of the first and second fluids Fi, F ₂ takes place to produce the intermediate fluid mixture F12, which in the second mixing chamber 40, together with the third fluid F3 (and further fluids), is subjected to a quasi-laminar mixing (degree of turbulence less than 0.1) with low shear rates.

The first process steps, designated P1.1, P2.1, and P3.1 in Figure 13, relate to the first fluid F1 and will take place in parallel with the process steps P1.2, P2.2, which relate to the second fluid _F2 , as well as with the process steps P1.3 and P2.3, which relate to the third fluid _F3 . Depending on the design, these can also take place in parallel with the optional process steps P1.4 and P2.4, which relate to other fluids.

During the process steps mentioned, the first fluid Fi, the second fluid F ₂ , the third fluid F3 (and the other fluids) are present in separate form.

First, in process steps P1.1, P1.2 and P1.3 (and optionally P1.4), the volume flow (flow rate) of the first fluid Fi, the second fluid _F2 and the third fluid F3 (and the other fluids) is set. Depending on the mixing ratio of fluid Fi and fluid _F2 , their volume flows are adjusted. In the event that during the mixing process If particles are generated, the particle size can also be influenced and adjusted by the ratio of the volume flows.

The ratio between the flow rate of the first fluid Fi and the flow rate of the second fluid F2 is greater than or equal to 1:1 (e.g., 1:1, 2:1, 3:1, 4:1, 5:1, 6:1, 7:1, 8:1, 9:1, or 10:1, and values therebetween). In other cases, the ratio between the flow rate of the second fluid F2 and the flow rate of the first fluid Fi is greater than 1:1 (e.g., 1:1, 2:1, 3:1, 4:1, 5:1, 6:1, 7:1, 8:1, 9:1, or 10:1, and values therebetween).

In the subsequent process steps P2.1, P2.2 and P2.3 (and optionally P2.4), the inlet pressure of the first fluid Fi (at the inlet opening 101 of the fluidic component 10), the inlet pressure of the second fluid F2 (at the second inlet opening 202 of the first mixing chamber 20), the inlet pressure of the third fluid F3 (at the second inlet opening 402 of the second mixing chamber 40) (and optionally the inlet pressures of the further fluids) are adjusted using suitable pumping devices (depending on the quantity, for example syringe pumps, multi-piston pumps, diaphragm pumps, gear pumps, circulation pumps, peristaltic pumps or other positive displacement pumps). The first, second and third fluids Fi, F ₂ , F ₃ (and optionally further fluids) are fed into the first, second and third feed devices 60, 70, 80 (and optionally further feed devices).

After the first fluid Fi has been introduced into the first supply device 60, the flow properties of the first fluid Fi are adjusted with the aid of the supply devices 60 in method steps P3.1. In P3.1, an oscillation of the first fluid Fi is generated with the aid of the fluidic component 10. The oscillation frequency is generally higher than 100 Hz. An oscillation frequency of several thousand Hz, such as 2000 Hz, is advantageous. Since the oscillation frequency can vary considerably depending on the size of the fluidic component 10, it is customary to specify the oscillation frequency dimensionlessly as a Strouhal number (St). For this purpose, the oscillation frequency f is divided by the average velocity U102 at the outlet opening 102 of the fluidic component 10 and multiplied by the width b2 of the outlet opening 102 of the fluidic component 10, St = f * bio2/U102. The Strouhal number defined in this way can be in the range 0.001 < St < 1, preferably 0.005 < St < 0.5 and particularly preferably 0.01 < St < 0.05. Thus, a passively oscillating first fluid Fi is provided at the outlet opening 102 of the fluidic component 10. The oscillation angle α of the first fluid Fi can be at least 5°, preferably at least 25°, particularly preferably at least 40°. For many applications, a Oscillation angles between 25° and 50° are suitable, especially between 30° and 45°. A typical maximum value for the oscillation angle is 75°.

In method step P4, the oscillating first fluid jet Fi, which is provided by the first supply device 60, and the (quasi-)stationary second fluid jet F ₂ , which is provided by the second supply device 70, are guided via the first and second inlet openings 201, 202 into the first mixing chamber 20, respectively, and combined there to form the intermediate fluid mixture F12. The collision occurs at the angles ß and q, which were already explained in more detail above in connection with the device 1. When the method is used on an industrial production scale or in mass production, the first and second fluids Fi, F ₂ are guided into the first mixing chamber 20 with a continuous volume flow.

In process step P5, the fluid mixture F12, which exits the first mixing chamber 20 via its outlet opening 203 at the end of the mixing process P4, is passed into a downstream first interaction channel 30 of length I30, in which the mixing continues until, after a characteristic mixing time tmix, a sufficiently homogeneous mixture of the two fluids Fi, _F2 is present. If particles (e.g., lipid nanoparticles, polymer nanoparticles, liposomes) or crystals have formed during the mixing process P4, they have time to mature in the first interaction channel 30.

The intermediate fluid mixture F12 emerging from the first interaction channel 30 is directed into the second mixing chamber 40 in process step P6.1 and combined with the third fluid F3 (and optionally the other fluids one after the other). The third fluid F3 and the other fluids can be different or identical.

To achieve gentle mixing, the third fluid F3 and the intermediate fluid mixture F12 are combined under specific fluid-mechanical criteria, which are demonstrated below using various exemplary embodiments. To keep the shear rates in the second mixing chamber 40 as low as possible, the velocities of the third fluid F3 and the intermediate fluid mixture _F12 must be as similar as possible in terms of magnitude and direction. If particles were formed during the mixing process P4, process step P6.1 can serve to stabilize the particles. Gentle mixing with low shear rates minimizes the mechanical stress on the particles, thereby achieving better particle quality. In one embodiment, increased stability of the particles (e.g., lipid nanoparticles) is achieved by diluting the particle stream (intermediate fluid mixture F12) with an aqueous solution, e.g., buffer solution (third fluid F3). In some process variants, the diluting fluid (third fluid _F3 ) is the same buffer solution used in the first fluid F1. In some process variants, the diluting fluid (third fluid F3) differs from the buffer solution used in the first fluid F1. In this case, the solvent content of the intermediate fluid mixture F12 is reduced, which leads to increased stability of the nanoparticles. For some nanoparticles, a solvent content of less than 50% leads to increased particle stability. In another embodiment, a solvent content of less than 25% leads to increased nanoparticle stability. In another embodiment, a solvent content of less than 10% leads to increased nanoparticle stability.

In one embodiment, the stability of the particles (e.g. lipid nanoparticles) is increased by increasing, decreasing or neutralizing the pH value of the particle stream (intermediate fluid mixture F12) from mixing process P4 by diluting it with an appropriate medium (third fluid _F3 ) (e.g. by acidic or basic buffer solution).

In one embodiment, the stability of the particles (e.g., polymer nanoparticles) is increased by adding a diluting medium (third fluid _F3 ) containing a surfactant to the particle stream (intermediate fluid mixture F12) from mixing process P4. The surfactant can be, for example, polyaxamers or polyvinyl alcohols, but is not limited to these substances.

In one embodiment, the aforementioned embodiments can be combined, whereby several fluids (e.g., two; but not limited to two) are successively fed to the particle stream (intermediate fluid mixture F12) from mixing process P4. For example, the third fluid _F3 is first fed to the particle stream before another fluid is fed to the resulting fluid mixture F123.

The ratio between the flow rate of the intermediate fluid mixture F12 and the flow rate of the third fluid _F3 is greater than or equal to 1:1 (e.g. 1:1, 2:1, 3:1, 4:1 or 5:1 and values in between). In other cases, the ratio between the flow rate of the third fluid F ₃ and the flow rate of the intermediate fluid mixture F12 is greater than 1:1 (e.g. 2:1, 3:1, 4:1 or 5:1 and values in between).

In process step P7.1, the fluid mixture F123, which exits from the second mixing chamber 40 via its outlet opening 403 at the end of the mixing process P6.1, is passed into a downstream second interaction channel 50 of length I50, in which the mixing from the second mixing chamber 40 is continued.

This second mixing process in the second mixing chamber 40 can be cascaded (optional process steps P6.2 and P7.2) by arranging several second mixing chambers 40 (optionally combined with a second interaction channel 50). In P6.2 and P7.2, analogous to P6.1 and P7.1, one or more additional fluids are combined with the fluid mixture generated from the previous mixing process. The fluids added in the optional steps can be identical to or different from the third fluid F3.

Process step P7.1 (optionally P7.2) is followed by process step P8, in which the produced fluid mixture is removed from the device 1. Process step P8 can be followed by a thermal treatment (e.g., cooling) of the produced fluid mixture and/or the separation of a component (e.g., a solvent) from the fluid mixture.

To carry out the process, process parameters must be defined. These depend on the size of the device. The size of the device influences the fluid velocity, which imposes limitations on the volume flow. The device shown in Figure 1 serves as a reference, wherein the first inlet opening 201 of the first mixing chamber has a width b ₂ oi and a height h ₂ oi, where h ₂ oi = b ₂ oi -

The volume flows of the other fluid flows then result from the respective ratios of the volume flows for certain embodiments of the process.

The figures depict various embodiments of the device 1, each corresponding to a specific combination of fluidic component 10, first mixing chamber 20, first interaction channel 30, second mixing chamber 40, and second interaction channel 50. Beyond the specific combinations depicted, the components of the individual embodiments can be combined with one another. It is also conceivable to omit the second interaction channel.

Different types of fluidic components can be used. These can include bypass channels or other means for targeted direction change.

In the description, the terms height h and depth t are used synonymously for the extension transverse to the oscillation plane of the first fluid.

Reference symbol

Fi first fluid

F2 second fluid

F ₃ third fluid

F12 intermediate fluid mixture

F123 Fluid mixture

Ri first fluid flow direction

R2 second fluid flow direction

R3 third fluid flow direction

R12 Fluid mixture flow direction

1 Device for generating a fluid mixture

10 fluidic component

11a, 11b inner blocks

100 flow chamber

101 Inlet opening

102 Outlet opening

103 Main stream channel

104a, 104b bypass duct

106 Approach

107 Exhaust port

20 first mixing chamber

201 first inlet opening

202 second inlet opening

203 Outlet opening

206 Inlet channel

207 exhaust duct

30 first interaction channel

301 Inlet opening

302 exhaust opening

303 Deflection

304 Deflection 305, 307, 308 Sections of the first interaction channel

40 second mixing chamber

401 first inlet opening

402 second inlet opening

403 exhaust opening

50 second interaction channel

501 Inlet opening

502 outlet opening

60 first feed device

70 second feed device

701 supply channel

80 third feed device

801 Supply channel

Claims

Patent claims 1. Device (1) for generating a fluid mixture comprising a first mixing chamber (20) with a first inlet opening (201) through which a first fluid (Fi) can be introduced into the first mixing chamber (20) along a first fluid flow direction (Ri), a second inlet opening (202) through which a second fluid (F ₂ ) can be introduced into the first mixing chamber (20) along a second fluid flow direction (R ₂ ), and an outlet opening (203) through which an intermediate fluid mixture (F12) comprising the first fluid (Fi) and the second fluid (F ₂ ) can be discharged along a fluid mixture flow direction (R12), wherein upstream of the outlet opening (203) an outlet channel (207) is formed, the cross-sectional area of which, which is defined transversely to the fluid mixture flow direction (R12), extends along the fluid mixture flow direction (R12) in the direction of the outlet opening (203), a second mixing chamber (40) with a first inlet opening (401), via which the intermediate fluid mixture (F12) can be introduced into the second mixing chamber (40) along the fluid mixture flow direction (R12), a second inlet opening (402), via which a third fluid ( _F3 ) can be introduced into the second mixing chamber (40) along a third fluid flow direction ( _R3 ), and an outlet opening (403), via which the fluid mixture ( _Fi23 ) comprising the first fluid (Fi), the second fluid ( _F2 ) and the third fluid ( _F3 ) can be discharged, and a first supply device (60) which is fluidically connected to the first mixing chamber (20) via the first inlet opening (201) and is designed to conduct the first fluid (Fi) along the first fluid flow direction (Ri) into the first mixing chamber (20), wherein the first supply device (60) comprises a fluidic component (10) which has • an outlet opening (102) which is fluidically connected to the first inlet opening (201) of the first mixing chamber (20), and • at least one means (104a, 104b) for the targeted change of direction of the first fluid (Fi) flowing through the fluidic component (10) to form a spatial oscillation of the first fluid (Fi) at the outlet opening (102), wherein the means (104a, 104b) for the targeted change of direction of the first fluid (Fi) is designed to bring about an oscillation of the first fluid (Fi) in an oscillation plane, a second supply device (70) which is fluidically connected to the first mixing chamber (20) via the second inlet opening (202) and is designed to second fluid (F ₂ ) along the second fluid flow direction (R ₂ ) into the mixing chamber (20), and a third supply device (80) which is fluidically connected to the second mixing chamber (40) via the second inlet opening (402) and is designed to supply the third fluid (F ₃ ) along the third fluid flow direction (R ₃ ) into the second mixing chamber (40), wherein the third supply device (80) has a supply channel (801 ) which extends along the third fluid flow direction (R ₃ ) and opens into the second inlet opening (402) of the second mixing chamber (40), wherein the supply channel (801 ) extends in a plane which is parallel to the oscillation plane, wherein a first interaction channel (30) is arranged between the first mixing chamber (20) and the second mixing chamber (40), which first interaction channel (30) connects the outlet opening (203) of the first Mixing chamber (20) and the first inlet opening (401) of the second mixing chamber (40) and which has a cross-sectional area transverse to the fluid mixture flow direction (R12) which is constant at least over a section immediately downstream of the outlet opening (203) of the first mixing chamber (20). 2. Device (1) according to claim 1, characterized in that the first interaction channel (30) has a section in which the cross-sectional area increases downstream transversely to the fluid mixture flow direction (R12). 3. Device (1) according to claim 1 or 2, characterized in that the third supply device (80) is provided and designed to guide the third fluid (F ₃ ) as a (quasi)stationary flow into the second mixing chamber (40). 4. Device (1) according to one of the preceding claims, characterized in that the supply channel (801) is rectilinear. 5. Device (1) according to one of the preceding claims, characterized in that the first supply device (60) is designed to bring about the targeted change in direction of the first fluid (Fi), so that the first fluid (Fi) moves within the first mixing chamber (20) in a time-varying manner, wherein the first fluid (Fi) has a movement component along the first fluid flow direction (Ri) and a movement component transverse to the first fluid flow direction (Ri), wherein the first fluid (Fi) moves within the first mixing chamber (20) in a time-varying manner, in particular periodically. 6. Device according to one of the preceding claims, characterized in that the fluidic component (10) comprises a flow chamber (100) through which the first fluid (Fi) can flow and which has a main flow channel (103) which connects an inlet opening (101) of the fluidic component (10) and its outlet opening (102) to one another, and at least one secondary flow channel (104a, 104b) as a means for the targeted change of direction of the first fluid (Fi). 7. Device (1) according to one of the preceding claims, characterized in that the first mixing chamber (20) has a longitudinal axis (L) which extends along the first fluid flow direction (Ri), and in that the cross-sectional area of the mixing chamber (20), which is defined transversely to the longitudinal axis (L), increases with increasing distance from the first inlet opening (201) of the first mixing chamber (20) in an upstream end section of the first mixing chamber (20) forming an inlet channel (206). 8. Device (1) according to one of the preceding claims, characterized in that a second interaction channel (50) is connected to the outlet opening (403) of the second mixing chamber (40). 9. Device (1) for generating a fluid mixture comprising a first mixing chamber (20) with a first inlet opening (201) through which a first fluid (Fi) can be introduced into the first mixing chamber (20) along a first fluid flow direction (Ri), a second inlet opening (202) through which a second fluid (F ₂ ) can be introduced into the first mixing chamber (20) along a second fluid flow direction (R ₂ ), and an outlet opening (203) through which an intermediate fluid mixture (F12) comprising the first fluid (Fi) and the second fluid (F ₂ ) can be discharged along a fluid mixture flow direction (R12), a second mixing chamber (40) with a first inlet opening (401) through which the intermediate fluid mixture (F12) can be introduced into the second mixing chamber (40) along the fluid mixture flow direction (R12), a second inlet opening (402), via which a third fluid (F ₃ ) can be introduced into the second mixing chamber (40) along a third fluid flow direction (R ₃ ), and an outlet opening (403), via which the fluid mixture (Fi ₂₃ ) comprising the first fluid (Fi), the second fluid (F ₂ ) and the third fluid (F ₃ ) can be discharged, a first supply device (60) which is fluidically connected to the first mixing chamber (20) via the first inlet opening (201) and is designed to guide the first fluid (Fi) along the first fluid flow direction (Ri) into the first mixing chamber (20), wherein the first supply device (60) comprises a fluidic component (10) which has • an outlet opening (102) which is fluidically connected to the first inlet opening (201) of the first mixing chamber (20), and • at least one means (104a, 104b) for the targeted change in direction of the first fluid (Fi) flowing through the fluidic component (10), in particular for forming a spatial oscillation of the first fluid (Fi) at the outlet opening (102), wherein the first inlet opening (401) of the second mixing chamber (40) has a cross-sectional area transverse to the fluid mixture flow direction (RI ₂ ) that is smaller than the cross-sectional area of the second inlet opening (402) of the second mixing chamber (40), wherein the cross-sectional area of the second inlet opening (402) of the second mixing chamber (40) is defined transversely to the third fluid flow direction (R ₃ ) and/or wherein the sum of the cross-sectional area of the first inlet opening (401) of the second mixing chamber (40) and the cross-sectional area of the second inlet opening (402) of the second mixing chamber (40) is similar to or larger than the cross-sectional area of the outlet opening (403) of the second mixing chamber (40). 10. Device (1) according to claim 9, characterized in that the means (104a, 104b) for the targeted change of direction of the first fluid (Fi) is designed to bring about an oscillation of the first fluid (Fi) in an oscillation plane. 11. Device (1 ) according to claim 10, characterized in that the second mixing chamber (40) has an extension parallel to the oscillation plane and transverse to the fluid mixture flow direction (RI ₂ ) which is constant. 12. Device (1) according to claim 10 or 11, characterized in that the second mixing chamber (40) has an extension parallel to the oscillation plane and transverse to the fluid mixture flow direction (RI ₂ ) which is the same size as the extension parallel to the oscillation plane and transverse to the fluid mixture flow direction (RI ₂ ) of the outlet opening (203) of the first mixing chamber (20) and/or the first inlet opening (401) of the second mixing chamber (40). 13. Device (1) according to one of claims 10 to 12, characterized in that the second mixing chamber (40) has an extension transverse to the oscillation plane which is greater than the extension of the first inlet opening (401) of the second mixing chamber (40) transverse to the oscillation plane. 14. Device (1) according to one of the preceding claims, characterized in that the device (1) further comprises: a second supply device (70) which is fluidically connected to the first mixing chamber (20) via the second inlet opening (202) and is designed to guide the second fluid (F ₂ ) along the second fluid flow direction (R ₂ ) into the mixing chamber (20), and a third supply device (80) which is fluidically connected to the second mixing chamber (40) via the second inlet opening (402) and is designed to guide the third fluid (F ₃ ) along the third fluid flow direction (R ₃ ) into the second mixing chamber (40). 15. Device (1) according to one of claims 9 to 14, characterized in that the first supply device (60) is designed to bring about the targeted change in direction of the first fluid (Fi), so that the first fluid (Fi) moves within the first mixing chamber (20) in a time-varying manner, wherein the first fluid (Fi) has a movement component along the first fluid flow direction (Ri) and a movement component transverse to the first fluid flow direction (Ri), wherein the first fluid (Fi) moves within the first mixing chamber (20) in a time-varying manner, in particular periodically. 16. Device according to one of claims 9 to 15, characterized in that the fluidic component (10) comprises a flow chamber (100) through which the first fluid (Fi) can flow and which has a main flow channel (103) which connects an inlet opening (101) of the fluidic component (10) and its outlet opening (102) to one another, and at least one secondary flow channel (104a, 104b) as a means for the targeted change of direction of the first fluid (Fi). 17. Device (1) according to one of claims 9 to 16, characterized in that the first mixing chamber (20) has a longitudinal axis (L) which extends along the first fluid flow direction (Ri), and in that the cross-sectional area of the first mixing chamber (20), which is defined transversely to the longitudinal axis (L), starting from the first inlet opening (201) of the first mixing chamber (20) in a Inlet channel (206) forming upstream end portion of the first mixing chamber (20) with increasing distance from the first inlet opening (201) increases and/or that the cross-sectional area in a downstream end section of the first mixing chamber (20) forming an outlet channel (207) decreases with increasing distance from the first inlet opening (201). 18. Device (1) according to claim 10 and claim 17, characterized in that the extension of the first mixing chamber (20) in the oscillation plane and transversely to the longitudinal axis (L) starting from the first inlet opening (201) of the first mixing chamber (20), in particular downstream of the second inlet opening (202) of the first mixing chamber (20), in the inlet channel (206) increases with increasing distance from the first inlet opening (201) or that the extension of the first mixing chamber (20) in the oscillation plane and transversely to the longitudinal axis (L) in the outlet channel (207) decreases with increasing distance from the first inlet opening (201). 19. Device (1) according to one of claims 9 to 18, characterized in that a first interaction channel (30) is arranged between the first mixing chamber (20) and the second mixing chamber (40), which first interaction channel (30) connects the outlet opening (203) of the first mixing chamber (20) and the first inlet opening (401) of the second mixing chamber (40) to one another and which in particular has a cross-sectional area transverse to the fluid mixture flow direction (RI ₂ ) which is constant at least in sections. 20. Device (1) according to claim 19, characterized in that the first interaction channel (30) has a smaller cross-sectional area transverse to the fluid mixture flow direction (R12) than the second mixing chamber (40). 21. Device (1) according to claim 10 and according to one of claims 19 and 20, characterized in that the first interaction channel (30) has an extension transverse to the oscillation plane which is smaller than the corresponding extension of the second mixing chamber (40), wherein in particular the extension of the first interaction channel (30) parallel to the oscillation plane and transverse to the fluid mixture flow direction (RI ₂ ) and the corresponding extension of the second mixing chamber (40) are of the same size. 22. Device (1 ) according to claim 10 and according to one of claims 19 to 21 , characterized in that the first interaction channel (30) has an extension transverse to the oscillation plane which is smaller than the extension parallel to the oscillation plane and transverse to the fluid mixture flow direction (RI ₂ ). 23. A method for producing a fluid mixture comprising the following steps: - Providing a device (1 ) according to one of claims 1 to 22, a first fluid (Fi), a second fluid (F ₂ ) and a third fluid (F ₃ ), - simultaneous introduction of the first fluid (Fi) with a first volume flow via the first supply device (60) into the first mixing chamber (20), of the second fluid (F ₂ ) with a second volume flow via the second supply device (70) into the first mixing chamber (20) and of the third fluid (F ₃ ) with a third volume flow via the third supply device (80) into the second mixing chamber (40), and - Discharging the fluid mixture (FI ₂₃ ) comprising the first fluid (Fi), the second fluid (F ₂ ) and the third fluid (F ₃ ) from the second mixing chamber (40) via its outlet opening (403). 24. Method according to claim 23, characterized in that the first volume flow is greater than the second volume flow or that the first volume flow and the second volume flow are equal. 25. The method according to claim 23 or 24, characterized in that the intermediate fluid mixture (FI ₂ ) enters the second mixing chamber (40) with a volume flow which is greater than the third volume flow or equal to the third volume flow. 26. Method according to one of claims 23 to 25, characterized in that the introduction of the first fluid (Fi) into the first mixing chamber (20), the introduction of the second fluid (F ₂ ) into the first mixing chamber (20) and the introduction of the third fluid (F ₃ ) into the second mixing chamber (40) each take place continuously. 27. Method according to one of claims 23 to 26, characterized in that the first fluid (Fi) and the third fluid (F ₃ ) are identical or different. 28. Method according to one of claims 23 to 27, characterized in that the third fluid (F ₃ ) is used to adjust a pH value, a particle density or a solvent content in the intermediate fluid mixture (F12) and/or comprises a surface-active substance. 29. Method according to one of claims 23 to 28, characterized in that the first fluid (Fi) and the second fluid (F2) differ in chemical Composition and/or concentration of individual components may differ. 30. Method according to one of claims 23 to 29, characterized in that the first fluid (F1) comprises an aqueous buffer solution, in particular in combination with one or more nucleic acids, and in that the second fluid (F2) comprises a polymer, a pharmaceutical active ingredient or a polymer-active ingredient conjugate or a lipid, in each case in a solvent.