KR101041045B1 - Micro reactors and process systems using them - Google Patents

Abstract

Micro reactors are provided.

Micro reactor according to the invention the inlet channel; A diverging channel connected to the center of one side of the inlet channel and dispersing a fluid flowing from the inlet channel on a plane; And a microchannel connected to the other side of the diverging channel, into which the fluid dispersed in the diverging channel flows, wherein the fluid movement length of the microchannel far from the other center of the diverging channel is the other center of the diverging channel. It is shorter than the fluid travel length of the microchannel at a short distance from the microchannel, and as a result, the microreactor according to the present invention enables the fluid flow at a uniform flow rate while maintaining sufficient energy efficiency. Therefore, the reactants flowing through the microchannels into the mixing zone generate the same heat transfer and mass transfer for each microchannel, thereby making it easier for the user to control the process.

Description

Microreactor and processing system using the same

The present invention relates to a microreactor and a process system using the same, and more particularly, to a microreactor having a high energy efficiency and a uniform velocity distribution and a process system using the same.

The microreactor may be defined as a miniaturized reaction system manufactured by applying microtechnology and precision engineering developed with the development of the electronic industry. Microreactors have fundamental advantages, such as excellent material and heat transfer properties, and uniform fluid flow, as well as the ability to scale-up lab-scale development without the need for scale-up. It is attracting much attention in the field of fine chemistry, where most of small quantity varieties are applied in that it can be directly applied to commercial production scale by applying the concept of simply increasing the number in parallel). The application of microreactors in the fine chemical process can be expected to provide several advantages in terms of chemical reactions. First, the microreactor is a continuous device with excellent mixing efficiency, and can be expected to increase yield and purity by maintaining a uniform reactant ratio and suppressing side reactions. The second is very fast heat exchange, which suppresses the formation of local hot spots, thereby minimizing the formation of by-products and thus increasing the selectivity of the reaction. Third, it is possible to control the ultra-precise process by the minute continuous process. Fourth, in terms of safety, it provides a safe process for using toxic or explosive reactants. In addition, as already mentioned in terms of commercial application, it is possible to apply commercialization immediately without the need for scale-up process, which is one of the heavy burdens in the process of commercializing fine chemicals. It can be easily responded to, and can be expected to have various advantages such as not requiring a large space in terms of location and easy installation in a narrow space. Attempts to develop chemical and biological processes using microreactors with many of these advantages are steadily spreading (Wolfgang Ehrfeld, Volker Hessel, Holger Lowe, Microreactors, Wiley-VCH, Weinheim, 2000).

That is, since the advantages of the microreactor described above can be effectively achieved by installing a plurality of parallel reactors and reacting, a microchannel parallel reactor having a plurality of channels is widely used as the microreactor. One way of such a microchannel reactor is a manifold type microchannel reactor, which is shown in FIG. 1.

Referring to FIG. 1, a general manifold type microchannel reactor has a structure in which an inlet channel is coupled to one side of a manifold, and a plurality of microchannels are coupled to the other side of the manifold. According to the above structure, the fluid flowing in the inflow channel is dispersed and introduced into the microchannel through the manifold. In such a microchannel reactor, the control of the flow rate in the microchannel is very important for achieving the effects of the microreactor such as the later mixing efficiency and heat transfer. That is, the non-uniform distribution of the flow rate can affect the performance of the microreactor in yield, selectivity, etc., and also cause a large change in mass transfer constant, and also change the residence time in the design value. However, in the conventional general microchannel reactor, the flow rate in the microchannel far from the inflow channel is slower than the flow rate of the near microchannel, which is caused by an increase in the distance and the resistance between the incoming fluid and the other side of the manifold. This is due to the pressure drop.

Another example of a microchannel reactor is a microreactor comprising a large volume inlet chamber provided between the inlet channel and the microchannel.

2 is a cross-sectional view of a conventional micro reactor having an inlet chamber.

Referring to FIG. 2, there is a large volume of inlet chamber 220 between inlet channel 210 and microchannel 230, which provides a large settling time for the incoming fluid, thereby providing an inlet channel. Reduce the pressure drop between 210 and microchannel 230. However, even in this case, the fluid flowing from the inflow channel 210 into the microchannel at a far distance still has a large pressure drop compared to the microchannel at the far distance, and as a result, the fluid flowing between the microchannels has an uneven flow rate. To have. Furthermore, in the inflow chamber 220, the flow of the fluid does not occur in the regions 220a and 220b that do not correspond to the direct path of the fluid, which may cause problems such as precipitation of the reactants.

3 is a cross-sectional view of a microreactor to avoid this problem of precipitation.

Referring to FIG. 3, the inflow chamber 320 has a radial structure in which a cross-sectional area is constantly increased toward the micro channel 330 from the inflow channel 310. That is, the fluid flow does not occur in the conventional inflow chamber 320 and thus removes the stagnant region from the inflow chamber, so that the fluid flow occurs in all regions of the inflow chamber 320. However, even in this case, since the distance from the inlet channel to each micro channel is different, the flow rate of the fluid flowing into the micro channel is different for each micro channel, which reduces the micro reactor efficiency.

Various types of reactors for controlling the flow rate of such microreactors are disclosed, and C. Amador discloses a reactor having a plurality of parallel structures (C. Amodor, A. Gavriilidis, P. Angeli, Flow distribution in different microreactors). scale-out geometries and the effect of manufacturing tolerances and channel blockage , Chemical Engineering Journal 101 (2004) 379-390).

4 is a sectional view of a reactor initiated by Amador.

Referring to FIG. 4, the fluid flowing from the inflow channel 410 flows through the plurality of microchannels 420 through a plurality of steps. That is, the micro-reactor initiated by Amador divides the incoming fluid into two flow paths instead of removing the inlet chamber, thereby providing a plurality of microchannels at the same time as the distance of the fluid path. Can be formed. However, in this case, the flowing fluid can cause a large amount of energy loss through a large number of splitting processes, which is uneconomical.

As described above, a microreactor capable of uniformizing the flow rate of the microchannel with sufficient energy efficiency in a microreactor, particularly a microreactor having a plurality of microchannels, has not been disclosed to date.

Accordingly, the first object of the present invention is to provide a micro reactor having high energy efficiency and having the same speed and pressure profile.

In addition, a second object of the present invention is to provide a chemical process system using the micro reactor.

The present invention in order to solve the above problems; A diverging channel connected to the center of one side of the inlet channel and dispersing a fluid flowing from the inlet channel on a plane; And a plurality of microchannels connected to the other side of the diverging channel, into which the fluid dispersed in the diverging channel flows.

The fluid flow length of the microchannel far from the center of the diverging channel is shorter than the fluid flow length of the microchannel of the distance from the other center of the diverging channel.

The difference in the fluid movement length of the plurality of microchannels in the above-described microreactor may be achieved by changing the position of the fluid inlet of the plurality of microchannels.

In addition, the microchannel is a rectangular duct type, the pressure of the fluid flowing into the microchannel is higher as the microchannel near the other center of the diverging channel, the pressure is determined by the following equation.

Where μ is the viscosity, Q is the flow rate, a is 1/2 of the height of the diverging channel, α is the angle of one side of the diverging channel with respect to the fluid flow direction, and r is the fluid of the microchannel with the inlet channel. Distance between inlets)

In addition, the pressure drop of the fluid occurs according to the following equation in the microchannel,

Where μ is the viscosity, L is the length of the microchannel, D _H is the hydraulic diameter, u _m is the average flow rate, and λ _NC is a non-circular factor)

In addition, the length step x formed by the distance between the microchannel and the inflow channel with respect to the fluid flow direction and the distance between the microchannel and the inflow channel that is closest to the center of the other side of the diverging channel is calculated by the following equation.

Where w is the width of the microchannel, e is the thickness of the microchannel, λ _NC is a non-circular factor, n is the number of microchannels, and α is the angle of one side of the diverging channel with respect to the direction of fluid flow, r ' _ref is the distance between the inlet and the inlet channel of the microchannel farthest from the center of the diverging channel, and r 'is the distance between the fluid inlet and the inlet channel of the microchannel)

In addition, the fluid in the microreactor is a lamina fluid.

In order to solve the second problem, the present invention provides a process system including one or more microreactors of the above type.

The process system according to the invention comprises at least two microreactors, wherein the microreactors can be configured in parallel. The process system according to the invention can also be applied to chemical or biological processes.

The present invention can provide a micro-reactor having a structure that can make the flow rate of the microchannel uniform while maintaining sufficient energy efficiency, so that the reactant flowing through the microchannel into the mixing region is the same for each microchannel. By generating heat transfer and mass transfer, the user's process control is easier.

The present invention is an inlet channel; A diverging channel connected to the center of one side of the inlet channel and dispersing a fluid flowing from the inlet channel on a plane; And a microchannel connected to the other side of the diverging channel and into which the fluid dispersed in the diverging channel flows, wherein the microchannel and the inflow of a distance from the center of the other side of the diverging channel are far from each other based on the fluid flow direction. The distance between the channels is shorter than the distance between the inlet channel and the microchannel of a close distance from the other center of the diverging channel provides a micro reactor.

Hereinafter, the microreactor according to the present invention will be described in detail with reference to the accompanying drawings.

5A and 5B are a cross-sectional view and a perspective view of the micro reactor according to the present invention.

5A and 5B, the micro reactor includes an inlet channel 510 and an inlet channel having a fan-shaped diverging channel for dispersing the fluid flowing from the inlet channel 510 into a larger area. A diverging channel 520 is included, and a plurality of micro channels 530 are connected to the other side of the diverging channel 520. In this case, since the microreactor is a planar microreactor, there is no vertical movement of the incoming fluid, and the fluid flowing in the diverging channel 520 is diffused and dispersed in one dimension, which will be described in more detail below.

Referring to the diverging channel 520 in detail, the diverging channel 520 is a fan shape having a uniform slope from the inlet channel 510 to the plurality of micro channels 530 in order to avoid problems such as stagnation (stagnation). The form is preferred. In this way, the pressure drop of the fluid according to the reactor structure can be kept to a minimum.

In addition, when looking at the micro-channel of the micro reactor according to the present invention, the micro-reactor connected to a distance farther to the center of the other side 520a than the inlet 530a of the microchannel connected to a distance close to the center of the micro-reactor other side (520a) The inlet portion 530b of the channel has a shorter fluid movement length. In the present invention, the fluid movement length is changed by changing the position of the inflow portion where the fluid enters the diverging channel instead of parallelizing the position of the outlet portion of the microchannel. Was different.

That is, the microchannel of the microreactor according to the present invention has a form in which the microchannel located far from the other center of the diverging channel is farther from the inflow channel based on the fluid flow direction than the microchannel located near the center thereof. As a result, the farther away from the other center of the diverging channel, the shorter the microchannel, and the shorter the moving length of the fluid.

As a result, the present invention uses the larger pressure drop of the above-described long path microchannel (center side) to distribute the flow rates among the microchannels equally. In the section, the fluid pressure is different. That is, the pressure of the fluid in the micro reactor according to the present invention is higher the closer the distance from the inlet channel, in the microchannel configuration according to the present invention, the inlet portion of the inner microchannel is higher than the outer microchannel inlet portion Have Accordingly, the present invention is characterized in that the pressure difference between the high pressure of the inner microchannel inlet and the low pressure of the outer microchannel inlet is compensated by the path difference between the microchannels, and as a result, the pressure between the microchannels. The car disappears and has the same pressure.

Thus, the same pressure that each microchannel will have at the same location will eventually equalize the flow rate of fluid flowing out of the microchannel and allow for effective process control of the user.

In addition, a process system employing the microreactor of the present invention with the same flow rate and flow rate is possible, which process may be chemical or biological.

As an example of such a process system, when using one microreactor, different reactions are performed for each of a plurality of microchannels having the same flow rate (this is, for example, mixing different reactants with different reactants into a common reactant flowing through each microchannel). It is possible to achieve this by means of a process system which produces different results for each microchannel.

As another example, a process system in which a plurality of micro reactors according to the present invention are installed in parallel is also possible. In any case, however, the process system according to the invention has the advantage of allowing homogeneous reactant inflow and mixing in the overall chemical reaction.

Thus, in the configuration of the micro reactor having the same flow rate in all the micro channels, it is very important to find the pressure of each micro inlet and the pressure drop in the micro channel, which will be described in detail below.

Micro Channel Inlet Pressure

The diverging channel according to the present invention can be described by the structure of the cylinder (r, θ, α) function.

6A-6C are front and side cross-sectional views of the diverging channel showing the function of the diverging channel of the present invention.

Referring to FIG. 6A, r denotes a distance from the inflow channel, θ denotes an angle from the central axis of the diverging channel, and α denotes an angle formed between the central axis of the diverging channel and the outer surface of the diverging channel.

6B and 6C, the angle formed by the outer surfaces 600a and 600b of the diverging channel is 2α, and the vertical height z of the diverging channel is defined as 2a. Also, the point at which the height z becomes zero is set to the middle of the diverging channel.

The fluid in contact with the wall of the diverging channel is stationary, i.e., no-slip. Furthermore, since the height of the channel in the z axis has a relatively small order range compared to the length scale of the other axes, the velocity distribution in the z-axis direction when the fluid flows sufficiently exhibits a parabolic shape. In addition, the fluid in the diverging channel exhibits a perfect gradient, where the velocity of the fluid particles in the vertical (z-axis direction) is zero and the velocity in the θ direction is also zero (v _θ = v _z = 0).

The continuous equation in this cylindrical form is shown in Equation 1 below.

That is, since rv _r is independent of r and v _r represents a parabola in the Z-axis direction, Equation 1 is a function of rv _r = θ, z = f (θ) (a ² -z ² ) Can be merged.

The f (θ) is determined by the solution of the Navier-Strokes equation, and since the velocity at the sidewall becomes 0 from the boundary state, θ = α: f (+ α) = f (−α) = 0 .

The flow rate is determined by the following equation.

It is possible to specify f (θ) for Q given from Equation 2, where the fluid diverging from the vertex represents a positive value, and the fluid converging toward the vertex is negative. Indicates the value of. Therefore, if Q defined by Equation 2 is a positive value, it represents an outflow of the fluid, and a negative value represents an inflow of the fluid.

일 때 Navier-Stokes 방정식의 r 및 θ 요소는 하기 수학식 3으로 표시된다.v _θ = 0

When r and θ elements of the Navier-Stokes equation is represented by the following equation (3).

Substituting the above equation for rv _r , the following equation (4) is obtained.

To remove pressure, The first expression of Equation 4 is differentiated with respect to θ, and the second equation is differentiated with respect to r, and the result is shown in Equation 5 below.

The following equation (6) can be obtained from the above equation.

This is a third-order ordinary differential equation that requires three conditions for f ( θ ) defined above, which is useful for representing independent, non-independent variables. The dimensionless angle Φ, the dimensionless flow rate variable F, and the dimensionless channel height ζ are defined as follows.

Φ is in a range between -1 and +1, and Equation 6 and Equation 2 regarding the boundary and surface states are represented by Equation 7 below.

일 때, R은 0이 된다. Where R represents the ratio of inertia (ρQ ² ) to viscosity stress (order of μQ), which plays a role similar to the Reynolds number. R also has a positive value or a negative value depending on whether it is an outflowing fluid or an incoming fluid. Also,

When R is 0.

In this diverging channel, the channel height is relatively small compared to r, so k _r has a positive value except near the vertex.

F and Φ have a unit size order, and furthermore, the change in F is a magnitude order unit, which appears as a change in φ of the unit order. Thus, the variable F is expected to be in unit size order f. Each F shown in the first equation of Equation 7 has a unit order multiplied by k _r α or R, whereby k _r α and R determine the relative importance of each variable in the first equation of Equation 7 above. Can be.

,

,

, 이 된다.In the diverging channel of the microreactor, the order of magnitude of each part of R is in SI units.

,

,

, Becomes.

In most chemical or biological reactions, the velocity of the fluid is significantly slower than subsonic, so the physical quantity order of R is significantly smaller than the unit value. Thus, since R is relatively small, the solution obtained by substituting 0 into R of the first equation of Equation 7 has a level of error that can be ignored. The equation obtained in this manner is as shown in Equation 8 below.

Now, the first equation of Equation 7, which is a nonlinear spin equation, becomes the second equation of Equation 7, which is a linear equation, and has an independent coefficient with respect to Φ, and the general equation is represented by Equation 9 below.

From the second and third terms of Equation 7, the equation of Equation 9 can be summarized as Equation 10 below.

In addition, Equation 10 can be rearranged by the following equation.

If the reactor has a long distance, no vertical motion can be present, and the effects of gravity can be ignored when calculating the pressure drop. Therefore, the pressure can be obtained by integrating the equation (5). However, considering the magnitude order of each term in Equation 5, the pressure can be simply obtained. First, the first equation of Equation 5 can be summarized as in Equation 12 below.

The magnitude order or range (SI unit) of each term of Equation 12 is

,

,

,

,

이다. 따라서, 상기 식의 우변의 첫 번째 및 두 번째 항은 상기 수학식 12의 세 번째 항보다 각각 10^-7 및 10^-6정도 적다. 따라서, 수학식 5의 두 번째 식에 따른 θ방향의 압력 강하의 차수는 10^-5 보다 적다.

,

,

,

,

to be. Thus, the first and second terms on the right side of the equation are 10 ⁻⁷ and 10 ⁻⁶ less than the third term in Equation 12, respectively. Therefore, the degree of pressure drop in the θ direction according to the second equation of Equation ⁵ is less than 10 ⁻⁵ .

Therefore, the rough pressure drop in the 3-direction can be summarized as in Equation 13 below.

The isobar of the diverging chamber from the above equation has an arc shape in which the distance r from the inlet of the diverging chamber (the point where the inlet channel is connected) becomes a radius. From the magnitude order analysis, the pressure drop in the r-direction in the divergence chamber is overwhelming, so the pressure in the θ -direction can be assumed to be the same as for θ = 0. Although f (θ) is not expressed as r, k but as a function of r, k _r can be replaced by k _∞ because it must have a positive value for any r, k. As a result, Equation 13 may be simply summarized by Equation 14 below.

Pressure drop in microchannel

Through the above-described method, the pressure of the microchannel inlet at the position of the distance r from the inlet can be obtained.

Therefore, it is necessary to find the pressure of the fluid generated with respect to the fluid flowing from the microchannel inlet to the microchannel with respect to the flow distance, which will be described in detail below.

The pressure drop relations all assume that the fluid flowing through the microchannel is a lamina fluid, and if the microchannel is circular, the pressure drop of the lamina fluid with an average velocity u _m can be measured using the Hagen-Poiseuille equation. Can be. However, non-circular channel is non-it is necessary to be included in the Hagen-Poiseuille equation for a circular parameter λ _NC and channel hydraulic diameter D _H is the pressure drop with the calculated, where λ _NC is a function e / w, this If the microchannel is in the form of a duct it is the ratio of the width and thickness of the duct (in the case of a circular channel the λ _NC = 1). Therefore, the pressure drop (length L, width w and thickness e) according to the Hagen-Poiseuille equation is summarized by Equation 15 below.

The hydraulic diameter D _H and the non-prototype factor λ _NC can be obtained from the following equation (16).

While passing through the microchannel, the average speed u _m may be converted to a flow rate as follows for convenience, and the pressure drop at this time is expressed by Equation 17 below.

delete

Calculation of the microchannel length according to the pressure drop

Referring to FIG. 7, the distance between the inlet 710 of the microchannel and the inlet channel 720 of the closest distance from the other center of the diverging channel is set to r ′ _ref and then derived from the above-described equation. According to Equation 18, the length step x in the fluid flow direction of the microchannel to be obtained for the closest microchannel is calculated.

Where w is the width of the microchannel, e is the thickness of the microchannel, λ _NC is a non-circular factor, n is the number of microchannels, α is the angle of one side of the diverging channel with respect to the direction of fluid flow, r ' _ref Is the distance between the inlet and the inlet channel of the microchannel nearest the distance from the center of the other side of the diverging channel, r 'is the distance between the fluid inlet and the inlet channel of the particular microchannel to obtain the projection distance x.

In this way, the pressures and flow rates of all the microchannels are the same from the point where the farthest microchannel starts from the other center of the diverging channel.

Example

The flow rate of the fluid flowing in the micro reactor according to the present invention was analyzed using a numerical analysis program (Computational Fluid Dynamics, CFD).

8a and 8b are graphs analyzed by CFD of the flow rate distribution for the microreactor according to the present invention.

In FIG. 8A, the arc in the diverging channel represents an isobar, and it can be seen that the pressure of the microchannel inlet inside the diverging channel is higher than the pressure of the microchannel inlet outside.

8B is a diagram showing the pressure distribution in the microchannels, and referring to FIG. 8B, it can be seen that the flow velocity is constant in all the microchannels.

In other words, the relatively high pressure at the inlet of the inner microchannel drops due to the pressure drop in accordance with the length difference, thereby making the same pressure between all the microchannels, and as a result, the flow rate distribution between the microchannels is the same.

Comparative example

9A and 9B show CFD analysis results for a micro reactor according to the related art.

9A, it can be seen that the pressure of the microchannel inlet coupled to the inside of the diverging channel, such as the microreactor according to the present invention, is higher than that of the microchannel inlet coupled to the outside.

However, referring to FIG. 9B, since the conventional microchannels have a constant length, the pressure difference cannot be attenuated, and the pressure difference appears in the same aspect throughout the microchannel.

1 is a cross-sectional view of a manifold-type microchannel reactor according to the prior art.

2 is a cross-sectional view of a conventional micro reactor.

3 is a cross-sectional view of another type of microreactor according to the prior art.

4 is a sectional view of a reactor initiated by Amador.

5A and 5B are a cross-sectional view and a perspective view of the micro reactor according to the present invention.

6A-6C are cross-sectional and side views, respectively, of the diverging channel according to the present invention.

FIG. 7 is a cross-sectional view illustrating a micro reactor having a micro channel inserted by a distance x according to an embodiment of the present invention.

8a and 8b are graphs analyzed by CFD of the flow rate distribution for the microreactor according to the present invention.

9A and 9B show CFD analysis results for a micro reactor according to the related art.

<Description of the symbols for the main parts of the drawings>

510 ..... influent channel 520 ..... divergent channel

530 ..... micro channel

Claims (10)

Inflow channel; A diverging channel connected to the center of one side of the inlet channel and dispersing a fluid flowing from the inlet channel on a plane; And a plurality of microchannels connected to the other side of the diverging channel, into which the fluid dispersed in the diverging channel flows. And the fluid movement length of the microchannel far from the center of the diverging channel is shorter than the fluid movement length of the microchannel of distance from the other center of the diverging channel. The method of claim 1, Wherein the difference in fluid travel length between the microchannels is achieved by varying the location of the fluid inlets of the plurality of microchannels. The method of claim 1, The micro-reactor is characterized in that the rectangular duct type. Inflow channel; A diverging channel connected to the center of one side of the inlet channel and dispersing a fluid flowing from the inlet channel on a plane; And a plurality of microchannels connected to the other side of the diverging channel, into which the fluid dispersed in the diverging channel flows. A fluid flow length of a microchannel far from the center of the diverging channel is shorter than a fluid flow length of the microchannel of a distance from the center of the diverging channel, wherein the fluid is a lamina fluid. The pressure of the fluid flowing into the micro channel is higher as the micro channel is closer to the other center of the diverging channel, wherein the pressure is determined by the following equation.

Where μ is the viscosity, Q is the flow rate, a is 1/2 of the height of the diverging channel, α is the angle of one side of the diverging channel with respect to the fluid flow direction, and r is the fluid of the microchannel with the inlet channel. Distance between inlets) Inflow channel; A diverging channel connected to the center of one side of the inlet channel and dispersing a fluid flowing from the inlet channel on a plane; And a plurality of microchannels connected to the other side of the diverging channel, into which the fluid dispersed in the diverging channel flows. The fluid movement length of the microchannel far from the center of the diverging channel is shorter than the fluid movement length of the microchannel of distance from the other center of the diverging channel, the fluid is a lamina fluid, and the microchannel As a rectangular duct type micro reactor, The pressure drop of the fluid in the micro channel is characterized in that according to the following formula.

Where μ is the viscosity, L is the length of the microchannel, D _H is the hydraulic diameter, u _m is the average flow rate, and λ _NC is a non-circular factor) Inflow channel; A diverging channel connected to the center of one side of the inlet channel and dispersing a fluid flowing from the inlet channel on a plane; And a plurality of microchannels connected to the other side of the diverging channel, into which the fluid dispersed in the diverging channel flows. The fluid movement length of the microchannel far from the center of the diverging channel is shorter than the fluid movement length of the microchannel of distance from the other center of the diverging channel, the fluid is a lamina fluid, and the microchannel As a rectangular duct type micro reactor, The length step x formed by the distance between the microchannel and the inflow channel and the distance between the microchannel and the inflow channel that are closest to each other from the center of the diverging channel based on the fluid flow direction is calculated by the following equation. Micro reactor.

Where w is the width of the duct, e is the thickness of the duct, λ _NC is a non-circular factor, n is the number of microchannels, α is the angle of one side of the diverging channel with respect to the direction of fluid flow, r ' _ref is The distance between the inflow channel and the inflow channel of the microchannel closest to the center of the diverging channel, and r 'is the distance between the fluid inflow section and the inflow channel of the specific microchannel for which the projection distance x is to be obtained.) The method of claim 1, And the fluid is a lamina fluid. Process system characterized in that it comprises at least one microreactor according to any one of the preceding claims. The method of claim 8, And at least two microreactors, wherein the microreactors are configured in parallel. The method of claim 8, Said process system being applicable to a chemical or biological process.

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