A three-dimensional microchannel reactor

Abstract

The present invention relates to the technical field of chemical engineering equipment, and discloses a three-dimensional microchannel reactor, which includes a reaction plate and a liquid outlet. A first reaction liquid inlet and a second reaction liquid inlet are further arranged in the reaction plate. The first reaction liquid inlet and the second reaction liquid inlet are connected to a mixing channel, and the mixing channel is communicated with the liquid outlet. A reaction channel groove is arranged on the mixing channel. The reaction channel groove includes a first reaction channel and a second reaction channel that divide the liquid in the mixing channel into two streams and are arranged in an upper and lower layer structure therebetween. The first reaction channel and the second reaction channel are periodically interconnected in an alternating manner; the reaction channel groove structure divides the mixed liquid into two streams, and enables the two streams of liquid to mix with each other at the cross-over overlapping structure. The cross-over overlapping structure not only exchanges the upper and lower layer positions of the first reaction channel and the second reaction channel, but also increases the diffusion of the liquid in the vertical direction, enhances the mixing effect, and thereby improves the reaction rate.

Description

Technical Field

[0001] The present invention relates to the technical field of chemical engineering equipment, and particularly to a three-dimensional microchannel reactor. Background Art

[0002] A microreactor, also known as a microchannel reactor, is a microreactor manufactured using precision machining technology with characteristic dimensions between 10 and 300 micrometers. Its core lies in controlling chemical reactions within a tiny space, such as in micrometer- or nanometer-scale channels, to achieve a more efficient and faster reaction process. Inside the microreactor, there are fluid flow channels with an equivalent diameter on the order of microns to millimeters, which provide an ideal place for chemical reactions. Its working principle is mainly based on the control of chemical reactions within a microscale space. By precisely controlling parameters such as reaction temperature, pressure, and the flow rate of materials, fine regulation of the reaction process can be achieved, thereby obtaining more stable and consistent products. In addition, the reaction materials in the microreactor can be quickly and evenly mixed, which helps to accelerate the reaction rate and improve reaction efficiency. Due to the usually small channel sizes (equivalent diameter in the order of microns and millimeters) and channel diversity in microreactors, fluids flow through these channels and are required to undergo the required reactions in these channels. This results in a very large surface area / volume ratio in microstructured chemical equipment.

[0003] However, the channel sizes of existing microreactors are usually in the range of microns to millimeters. Although such tiny sizes help to precisely control reaction conditions, they also limit the mixing ability of fluids. For example, linear, U-shaped, etc., may not be conducive to the full mixing of fluids. Especially when the reaction materials flow in a laminar state, the mass transfer between different fluid layers is restricted, resulting in poor mixing effects. For example, a microreactor proposed in Chinese Patent CN201710573286.6 includes a first reaction liquid inlet; a second reaction liquid inlet; a reaction liquid outlet; a reaction channel, the inlet is connected to the first reaction liquid inlet and the second reaction liquid inlet, and the outlet is connected to the reaction liquid outlet; reaction units, at least two, connected in series on the reaction channel, and the reaction units are composed of at least two grid plates stacked and staggered to form an interconnected channel structure. This structure has a weak mixing effect in reactions that require high-speed mixing. The molecules in the fluid mainly diffuse along the flow direction, while the diffusion speed perpendicular to the flow direction is slower, resulting in incomplete reactions. Summary of the Invention

[0004] (1) Technical problems to be solved: Aiming at the deficiencies of the prior art, the present invention provides a three-dimensional microchannel reactor, which has the advantages of good mixing effect and good mass transfer effect, and solves the problem of poor mixing effect of existing reactors.

[0005] (II) Technical solution: To achieve the above-mentioned purpose of good synthesis effect and good mass transfer effect, the present invention provides the following technical solution: a three-dimensional microchannel reactor, comprising a reaction plate and a liquid outlet, wherein a first reaction liquid inlet and a second reaction liquid inlet are further arranged in the reaction plate, wherein the first reaction liquid inlet and the second reaction liquid inlet are connected with a mixing channel, wherein the mixing channel is communicated with the liquid outlet, wherein a reaction channel groove is arranged on the mixing channel, wherein the reaction channel groove comprises a first reaction channel and a second reaction channel which divide the liquid in the mixing channel into two streams and are arranged in layers up and down therebetween, wherein the first reaction channel and the second reaction channel are periodically interlaced with each other, wherein a channel slope is arranged at the interlaced position of the first reaction channel and the second reaction channel, wherein the channel slope enables the first reaction channel and the second reaction channel to interchange the upper and lower positions at the interlaced position and enables the liquids in the reaction channel groove to mix with each other and then be diverted again.

[0006] Preferably, the size of the reaction channel groove changes periodically, the diameter of the first reaction channel and the second reaction channel decreases at the staggered position, and the diameter of the first reaction channel and the second reaction channel increases at the non-staggered position.

[0007] Preferably, the combination of the first reaction channel and the second reaction channel is in the shape of a spindle structure, the spindle structure is arranged along the reaction channel groove array, and the width of the spindle structure increases and decreases periodically.

[0008] Preferably, the height of the spindle structure increases and decreases periodically, and the width and height of the spindle structure are adjustable.

[0009] Preferably, the first reaction channel and the second reaction channel are provided with a cross-overlapping structure for mixing liquids at staggered positions, and the cross-overlapping structure makes the first reaction channel and the second reaction channel partially overlap, and the channel slope is provided on the cross-overlapping structure.

[0010] Preferably, the width of the first reaction channel is equal to the width of the second reaction channel.

[0011] Preferably, the vertical height of the channel slope is greater than half of the width of the first reaction channel, and the liquid crosses and impacts each other when passing through the channel slope, mixes, and then separates into two streams of liquid that enter the first reaction channel and the second reaction channel respectively.

[0012] Preferably, the reaction channel grooves are arranged in two or more groups in a U-shape in the reaction plate.

[0013] Preferably, partitions are fixedly installed on both sides of the reaction plate, the liquid outlet passes through a single side of the reaction plate and is opened on the partition, and the first reaction liquid inlet and the second reaction liquid inlet pass through a single side of the reaction plate and are opened on the partition.

[0014] (3) Beneficial effects: Compared with the prior art, the present invention provides a three-dimensional microchannel reactor, which has the following beneficial effects:

[0015] 1. In this three-dimensional microchannel reactor, through the combined use of the reaction channel groove structure and the cross-overlapping structure, the reaction channel groove structure divides the mixed liquid into two streams, and at the cross-overlapping structure, the two liquid streams are mixed and collided with each other. The channel slopes provided at the cross-overlapping structure not only exchange the upper and lower layer positions of the first reaction channel and the second reaction channel, but also increase the diffusion of the liquid in the vertical direction, enhance the mixing effect, thereby improving the reaction rate. At the same time, the upper and lower channel slopes increase the contact area with the overall reaction plate, contributing to heat transfer and heat dissipation, and thus improving the heat exchange effect of the reaction channel groove.

[0016] 2. In this three-dimensional microchannel reactor, through the combined use of the spindle structure and the reaction channel groove structure, it can guide the flow of the liquid, reduce the resistance of the channel, and ensure that the liquid can fill the entire reaction channel groove. In addition, the narrower part of the spindle structure forms a jet effect to push the liquid forward, while the wider part provides a space for buffering and mixing of the liquid, effectively avoiding the occurrence of dead zones and improving the reaction efficiency.

[0017] 3. In this three-dimensional microchannel reactor, through the combined use of the reaction channel groove structure and the spindle structure, when the flow rate changes caused by the size changes of the first reaction channel and the second reaction channel are superimposed with the periodic changes of the spindle structure, their effects on the liquid flow rate will be superimposed on each other, thereby greatly improving the mixing rate of the liquid in the reaction channel groove. BRIEF DESCRIPTION OF THE DRAWINGS

[0018] Figure 1 is a three-dimensional structure schematic diagram of the three-dimensional microchannel reactor in the present invention;

[0019] Figure 2 is a structural sectional view of the three-dimensional microchannel reactor in the present invention;

[0020] Figure 3 is a three-dimensional structural sectional view of the three-dimensional microchannel reactor in the present invention;

[0021] Figure 4 is Figure 3 part A in

[0022] Figure 5 is a three-dimensional structure schematic diagram of the reaction channel groove in the present invention;

[0023] Figure 6 is a structural top view of the reaction channel groove in the present invention;

[0024] Figure 7 Front elevation view of the structure of the reaction channel groove in the present invention;

[0025] Figure 8 Front elevation view of the structure of the reaction channel groove in the present invention after the width of the spindle structure is adjusted.

[0026] In the figure: 1, reaction plate; 2, liquid outlet; 3, first reaction liquid inlet; 4, second reaction liquid inlet; 5, mixing channel; 6, reaction channel groove; 61, first reaction channel; 62, second reaction channel; 63, cross-overlapping structure; 631, channel slope; 64, spindle structure; 7, partition board. Detailed implementation manners

[0027] Next, the technical solutions in the embodiments of the present invention will be clearly and completely described in conjunction with the accompanying drawings in the embodiments of the present invention. Obviously, the described embodiments are only a part of the embodiments of the present invention, rather than all the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those of ordinary skill in the art without creative efforts shall fall within the protection scope of the present invention.

[0028] Please refer to Figures 1-8, A three-dimensional microchannel reactor, comprising a reaction plate 1 and an outlet 2. Inside the reaction plate 1, a first reaction inlet 3 and a second reaction inlet 4 are also provided. The first reaction inlet 3 and the second reaction inlet 4 are connected to a mixing channel 5, and the mixing channel 5 is communicated with the outlet 2. The first reaction inlet 3 and the second reaction inlet 4 are designed to be able to introduce two different reactants or solvents simultaneously. These two inlets are connected through the mixing channel 5, enabling the two liquids to be fully mixed within the mixing channel 5. The design of the mixing channel 5 ensures that the reactants reach a uniform mixing state before entering the reaction area. There is a reaction channel groove 6 on the mixing channel 5. The reaction channel groove 6 includes a first reaction channel 61 and a second reaction channel 62 that divide the liquid in the mixing channel 5 into two streams and are arranged in an upper and lower layered manner between them. The first reaction channel 61 and the second reaction channel 62 are periodically interconnected in an alternating manner. The design of the first reaction channel 61 and the second reaction channel 62 being periodically interconnected in an alternating manner is to achieve cross-mixing and redistribution of the liquid. This design enables the liquid to continuously change its flow direction and path when flowing through the reaction channels, thereby increasing the disturbance and mixing degree of the liquid. In addition, the alternating interconnection design can also avoid the occurrence of dead zones or stagnant zones in the reaction channels, ensuring that the reactants can fully participate in the reaction. There is a channel slope 631 at the alternating position of the first reaction channel 61 and the second reaction channel 62. The channel slope 631 causes the upper and lower layer positions of the first reaction channel 61 and the second reaction channel 62 to be interchanged at the alternating position and enables the liquid in the reaction channel groove 6 to be remixed and then redistributed. When the liquid flows through the channel slope 631, it will be guided and lifted by the slope, thereby changing the flow direction and increasing the diffusion in the vertical direction. This design not only helps to achieve full mixing of the liquid but also can improve the heat exchange efficiency of the reaction channel groove 6. Because the presence of the slope increases the contact area between the liquid and the reaction plate 1, which is conducive to heat transfer and dissipation. At the same time, the channel slope 631 can also play a role in regulating the liquid flow rate and flow state, further optimizing the performance of the reactor.

[0029] Please refer to Figures 3-7, the size of the reaction channel groove 6 changes periodically. The diameter of the first reaction channel 61 and the second reaction channel 62 decreases at the staggered positions, and the diameter increases at the non-staggered positions. The periodic change in the size of the reaction channel groove 6 helps to generate a periodic change in the flow velocity within the channel. At the positions where the diameter decreases, due to the reduction in the cross-sectional area of the channel, the flow velocity will increase, forming a jet effect, which helps to enhance the liquid mixing and reaction rate. At the positions where the diameter increases, the flow velocity slows down, providing a space for liquid buffering and mixing. The combined shape between the first reaction channel 61 and the second reaction channel 62 is a spindle structure 64. The spindle structure 64 is arranged in an array along the reaction channel groove 6, and the width of the spindle structure 64 changes periodically in increase and decrease. The height of the spindle structure 64 changes periodically in increase and decrease. The spindle height and width are adjustable as Figure 8 shown. The design of the spindle structure 64 helps to guide the flow direction of the liquid, causing it to form periodic acceleration and deceleration within the channel. At the narrower part of the spindle, the flow velocity will increase, forming a jet effect, which helps to push the liquid forward. At the wider part, the flow velocity slows down, providing a space for liquid buffering and mixing. Since both the width and height of the spindle structure 64 change periodically in increase and decrease, periodic disturbances and shear forces will be generated within the channel. These disturbances and shear forces can break the laminar flow structure in the liquid, promoting the uniform mixing and full reaction of the liquid.

[0030] Please refer to Figures 3-5, the first reaction channel 61 and the second reaction channel 62 are provided with an overlapping structure 63 for liquid mixing at an interleaved position, and the overlapping structure 63 causes partial overlap between the first reaction channel 61 and the second reaction channel 62. The channel slope 631 is provided on the overlapping structure 63. This design is mainly to enhance the liquid mixing effect and improve the reaction rate. In the overlapping structure 63, the first reaction channel 61 and the second reaction channel 62 partially overlap, enabling the two liquid streams to come into contact and mix with each other at the interleaved position. The setting of the channel slope 631 further promotes this mixing process. When the liquid flows through the channel slope 631, due to the guidance of the slope, the liquid will cross and counteract, forming strong turbulence and shear force, thereby enhancing the liquid mixing effect. The width of the first reaction channel 61 is equal to the width of the second reaction channel 62. Designing the width of the first reaction channel 61 to be equal to the width of the second reaction channel 62 is to ensure that the two liquid streams have equal flow rates and velocities at the interleaved position, which is conducive to the uniform mixing of the liquid. The vertical height of the slope of the channel slope 631 is greater than half of the width value of the first reaction channel 61. After the liquid crosses and counteracts each other when passing through the channel slope 631, it mixes and then separates into two liquid streams and enters the first reaction channel 61 and the second reaction channel 62 respectively. The vertical height of the slope of the channel slope 631 being greater than half of the width value of the first reaction channel 61 is to ensure that the liquid can undergo sufficient cross-counteraction when passing through the slope. If the vertical height of the slope is too small, the liquid may not be fully counteracted and mixed; while if the vertical height of the slope is too large, it may increase the flow resistance of the liquid and reduce the reaction rate. The reaction channel grooves 6 are arranged in two or more U-shaped groups within the reaction plate 1. The U-shaped arrangement can make full use of the area of the reaction plate 1 while ensuring that the liquid can be fully mixed and reacted within the reaction channel grooves 6. Partition plates 7 are fixedly installed on both sides of the reaction plate 1. The partition plates 7 are to ensure the sealing and stability of the reaction channel grooves 6. The liquid outlet 2 is opened on the partition plate 7 through a single side of the reaction plate 1, and the first reaction liquid inlet 3 and the second reaction liquid inlet 4 are opened on the partition plate 7 through a single side of the reaction plate 1.

[0031] Working principle: Two or more liquids are transported into the reaction plate 1 through the first reaction liquid inlet 3 and the second reaction liquid inlet 4 by a pump or other means. After that, they flow and mix through the mixing channel 5, and then through the reaction channel groove 6. The reaction channel groove 6 can divide the mixed liquid into two streams through the first reaction channel 61 and the second reaction channel 62. When the divided liquids flow in their respective channels, they will be restricted by the channel wall and affected by the channel shape, thus generating perturbations. This kind of perturbation helps to enhance the mixing effect of the liquids, improve the reaction rate. And because the combined shape between the first reaction channel 61 and the second reaction channel 62 presents a spindle structure 64, the spindle structure 64 is beneficial to guiding the liquid flow. The design of the spindle structure 64 makes the channel show periodic changes in width and height. In the narrower part of the spindle structure 64, the flow rate of the liquid will increase, forming a jet effect, which helps to push the liquid forward. While in the wider part, the flow rate slows down, providing a space for buffering and mixing of the liquid. The spindle structure 64 reduces the resistance of the channel and also ensures that the liquid can fill the entire reaction channel groove 6 and flow in the form of plug flow, thus avoiding the emergence of dead zones. When the liquid flows through the cross-over structure 63 of the reaction channel groove 6, the liquids in the first reaction channel 61 and the second reaction channel 62 can be mixed with each other. Then the two liquid streams cross again. And because there is partial channel overlap at the cross-over structure 63, the collision of the two liquid streams strengthens the perturbation degree and then divides into two liquids again. At the same time, channel slopes 631 are arranged in the first reaction channel 61 and the second reaction channel 62. The channel slopes 631 can make the upper and lower positions of the first reaction channel 61 and the second reaction channel 62 exchange, so that the liquids cross and collide at the cross-over structure 63. The channel slopes 631 can not only lift and lower the channels, making the upper and lower levels of the two channels change positions, but also increase the diffusion of the liquid in the vertical direction to increase the mixing effect. And the upper and lower channel slopes 631 can improve the heat exchange of the reaction channel groove 6 because they increase the contact area with the whole reaction plate 1.

[0032] At the same time, the changes in the sizes of the first reaction channel 61 and the second reaction channel 62 and the periodic changes in the spindle structure 64 will both affect the flow rate of the liquid. At the position where the diameter of the reaction channel groove 6 decreases, the flow rate of the liquid will increase, forming a jet effect. While at the position where the diameter increases, the flow rate slows down, providing a space for buffering and mixing of the liquid. This kind of change in the flow rate can cause effects such as buffering, jetting, oscillation, and backmixing, thus enhancing the mixing effect of the liquids. And when these two structural changes are superimposed on each other, their effects on the liquid flow rate will be superimposed on each other, thus greatly improving the mixing rate of the liquid in the reaction channel groove 6.

[0033] It should be noted that in this text, relational terms such as first and second are only used to distinguish one entity or operation from another entity or operation, and do not necessarily require or imply any actual relationship or order between these entities or operations. Moreover, the terms "comprising", "including" or any other variant thereof are intended to cover non-exclusive inclusion, such that a process, method, article or device comprising a series of elements not only includes those elements but also includes other elements not expressly listed, or elements inherent to such process, method, article or device. Without further limitation, an element defined by the phrase "comprising an..." does not exclude the presence of additional identical elements in the process, method, article or device comprising said element.

[0034] Although embodiments of the present invention have been shown and described, it will be understood by those of ordinary skill in the art that various changes, modifications, substitutions and variations can be made to these embodiments without departing from the principles and spirit of the invention, and the scope of the invention is defined by the appended claims and their equivalents.

Claims

1. A three-dimensional microchannel reactor, comprising a reaction plate (1) and a liquid outlet (2), wherein the reaction plate (1) is further provided with a first reaction liquid inlet (3) and a second reaction liquid inlet (4), wherein the first reaction liquid inlet (3) and the second reaction liquid inlet (4) are connected with a mixing channel (5), wherein the mixing channel (5) is connected with the liquid outlet (2), and a reaction channel groove (6) is provided on the mixing channel (5), characterized in that: The reaction channel groove (6) comprises a first reaction channel (61) and a second reaction channel (62) which divide the liquid in the mixing channel (5) into two streams and are arranged in layers up and down. The first reaction channel (61) and the second reaction channel (62) are interlaced with each other in a periodic manner. A channel slope (631) is arranged at the interlaced position of the first reaction channel (61) and the second reaction channel (62). The channel slope (631) enables the first reaction channel (61) and the second reaction channel (62) to interchange the upper and lower layer positions at the interlaced position and enables the liquid in the reaction channel groove (6) to be mixed and then re-divided.

2. A three-dimensional microchannel reactor according to claim 1, characterized in that: The size of the reaction channel groove (6) changes periodically, the diameter of the first reaction channel (61) and the second reaction channel (62) decreases at the staggered position, and the diameter of the first reaction channel (61) and the second reaction channel (62) increases at the non-staggered position.

3. A three-dimensional microchannel reactor according to claim 1, characterized in that: The combined shape of the first reaction channel (61) and the second reaction channel (62) is a spindle structure (64), the spindle structure (64) is arranged in an array along the reaction channel groove (6), and the width of the spindle structure (64) changes in a periodic manner.

4. A three-dimensional microchannel reactor according to claim 3, characterized in that: The height of the spindle structure (64) increases and decreases periodically.

5. A three-dimensional microchannel reactor according to claim 1, characterized in that: The first reaction channel (61) and the second reaction channel (62) are provided with a cross-overlapping structure (63) for mixing liquids at staggered positions, and the cross-overlapping structure (63) causes the first reaction channel (61) and the second reaction channel (62) to partially overlap, and the channel slope (631) is provided on the cross-overlapping structure (63).

6. A three-dimensional microchannel reactor according to claim 1, characterized in that: The width of the first reaction channel (61) is equal to the width of the second reaction channel (62), and the vertical height of the slope of the channel slope (631) is greater than half of the width of the first reaction channel (61). When the liquid passes through the channel slope (631), it crosses and impacts each other, mixes, and then separates into two streams of liquid, which respectively enter the first reaction channel (61) and the second reaction channel (62).

7. A three-dimensional microchannel reactor according to claim 1, characterized in that: The reaction channel grooves (6) are arranged in two or more groups in a U-shape in the reaction plate (1).

8. A three-dimensional microchannel reactor according to claim 1, characterized in that: Partitions (7) are fixedly mounted on both sides of the reaction plate (1); the liquid outlet (2) penetrates through a single side of the reaction plate (1) and is opened on the partition (7); and the first reaction liquid inlet (3) and the second reaction liquid inlet (4) penetrate through a single side of the reaction plate (1) and are opened on the partition (7).

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