Three-dimensional micro-channel reactor

Abstract

The invention relates to the technical field of chemical and chemical equipment, and discloses a three-dimensional microchannel reactor which comprises a reaction plate and a liquid outlet, a first reaction liquid inlet and a second reaction liquid inlet are further formed in the reaction plate and connected with a mixing channel, the mixing channel is communicated with the liquid outlet, and the liquid outlet is communicated with the first reaction liquid inlet and the second reaction liquid inlet. A reaction channel groove is formed in the mixing channel, the reaction channel groove comprises a first reaction channel and a second reaction channel which divide liquid in the mixing channel into two strands and are arranged in an up-and-down layered mode, and the first reaction channel and the second reaction channel are periodically and mutually communicated in a staggered mode; the reaction channel groove structure divides mixed liquid into two streams, the two streams of liquid are mutually mixed at the position of the crossed and overlapped structure, the crossed and overlapped structure not only enables the positions of the upper layer and the lower layer of the first reaction channel and the second reaction channel to be interchanged, but also increases diffusion of the liquid in the vertical direction, enhances the mixing effect, and further improves the reaction rate.

Description

Technical Field

[0001] The invention relates to the technical field of chemical equipment, in particular to a three-dimensional microchannel reactor. Background Art

[0002] Microreactors, also known as microchannel reactors, are microreactors with characteristic dimensions between 10 and 300 microns manufactured using precision machining technology. The core is to control chemical reactions in tiny spaces, such as micron or nanometer channels, to achieve more efficient and faster reaction processes. Microreactors contain fluid flow channels with equivalent diameters between microns and millimeters, which provide an ideal place for chemical reactions. Its working principle is mainly based on the control of chemical reactions in microscopic spaces. By accurately controlling parameters such as reaction temperature, pressure, and material flow, the reaction process can be finely regulated to obtain more stable and consistent products. In addition, the reaction materials in the microreactor can be mixed quickly and evenly, which helps to speed up the reaction rate and improve the reaction efficiency. Since microreactors usually contain small channel sizes (equivalent diameters of micrometers and millimeters) and channel diversity, fluids flow in these channels and require the required reactions to occur in these channels. This results in a very large surface area / volume ratio in microstructured chemical equipment.

[0003] However, the channel size of existing microreactors is usually in the micron to millimeter level. Although this tiny size helps to accurately control the reaction conditions, it also limits the mixing ability of the fluid. For example, straight-line, U-shaped, etc., may not be conducive to the full mixing of the fluid. In particular, when the reaction material flows in a laminar state, the material exchange between different fluid layers is limited, resulting in poor mixing effect. 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; a reaction unit, at least two, is connected in series on the reaction channel, and the reaction unit is stacked and staggered by at least two grid plates 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 rate perpendicular to the flow direction is slow, resulting in the reaction not being fully carried out. Summary of the invention

[0004] (I) Technical problems to be solved: In view of the deficiencies in the prior art, the present invention provides a three-dimensional microchannel reactor having the advantages of good mixing effect and good mass transfer effect, thereby solving the problem of poor mixing effect of the prior art reactor.

[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 staggered position and 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] (III) Beneficial effects: Compared with the prior art, the present invention provides a three-dimensional microchannel reactor having the following beneficial effects: 1. The three-dimensional microchannel reactor, through the coordinated use of a reaction channel trough structure and a cross-overlapping structure, the reaction channel trough structure divides the mixed liquid into two streams, and makes the two streams of liquid mix and collide with each other at the cross-overlapping structure. The channel slope surface arranged at the cross-overlapping structure not only makes the upper and lower layers of the first reaction channel and the second reaction channel interchangeable, but also increases the diffusion of the liquid in the vertical direction, enhances the mixing effect, and thereby increases the reaction rate. At the same time, the upper and lower channel slope surfaces increase the contact area with the reaction plate as a whole, which is helpful for the transfer and heat dissipation of heat, thereby improving the heat exchange effect of the reaction channel trough.

[0015] 2. This three-dimensional microchannel reactor, through the coordinated use of a spindle structure and a reaction channel groove structure, can guide the flow of 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, pushing the liquid forward, while the wider part provides a buffering and mixing space for the liquid, effectively avoiding the occurrence of dead zones and improving reaction efficiency.

[0016] 3. This three-dimensional microchannel reactor uses a reaction channel groove structure in conjunction with a spindle structure. When the flow rate changes caused by the size changes of the first reaction channel and the second reaction channel and the periodic changes of the spindle structure are superimposed on each other, 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

[0017] Figure 1 It is a schematic diagram of the three-dimensional structure of the three-dimensional microchannel reactor in the present invention.

[0018] Figure 2 It is a structural cross-sectional view of the three-dimensional microchannel reactor in the present invention.

[0019] Figure 3 It is a three-dimensional structural cross-sectional view of the three-dimensional microchannel reactor in the present invention.

[0020] Figure 4 for Figure 3 Part A.

[0021] Figure 5 It is a schematic diagram of the three-dimensional structure of the reaction channel groove in the present invention.

[0022] Figure 6 It is a top view of the structure of the reaction channel groove in the present invention.

[0023] Figure 7It is a structural front view of the reaction channel groove in the present invention.

[0024] Figure 8 It is a front view of the structure after the width of the spindle structure in the reaction channel groove of the present invention is adjusted.

[0025] 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. DETAILED DESCRIPTION

[0026] The following will be combined with the drawings in the embodiments of the present invention to clearly and completely describe the technical solutions in the embodiments of the present invention. Obviously, the described embodiments are only part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the present invention.

[0027] See also Figure 1-Figure 8A three-dimensional microchannel reactor comprises a reaction plate 1 and a liquid outlet 2. A first reaction liquid inlet 3 and a second reaction liquid inlet 4 are also provided in the reaction plate 1. The first reaction liquid inlet 3 and the second reaction liquid inlet 4 are connected with a mixing channel 5. The mixing channel 5 is connected with the liquid outlet 2. The first reaction liquid inlet 3 and the second reaction liquid inlet 4 are designed to be able to introduce two different reactants or solvents at the same time. The two liquid inlets are connected by the mixing channel 5 so that the two liquids can be fully mixed in the mixing channel 5. The design of the mixing channel 5 ensures that the reactants have reached a uniform mixing state before entering the reaction area. The mixing channel 5 is provided with a reaction channel groove 6. 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 strands and are arranged in layers up and down. The first reaction channel 61 and the second reaction channel 62 are interlaced and communicated with each other periodically. The design that the first reaction channel 61 and the second reaction channel 62 are interlaced and communicated with each other periodically is to achieve cross mixing and redistribution of the liquid. This design enables the liquid to continuously change the flow direction and path when flowing through the reaction channel, thereby increasing the disturbance and mixing degree of the liquid. In addition, the staggered design can also avoid the occurrence of dead zones or retention zones in the reaction channel, ensuring that the reactants can fully participate in the reaction. The first reaction channel 61 and the second reaction channel 62 are staggered at a channel slope 631, and the channel slope 631 allows the first reaction channel 61 and the second reaction channel 62 to interchange the upper and lower positions at the staggered position and to re-divide the liquid in the reaction channel groove 6 after mixing with each other. 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 improves 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, it is conducive to the transfer and dissipation of heat. At the same time, the channel slope 631 can also play a role in regulating the flow rate and flow state of the liquid, further optimizing the performance of the reactor.

[0028] See also Figure 3-Figure 7, the size of the reaction channel groove 6 changes periodically, the channel 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 staggered position and the non-staggered position. The size of the reaction channel groove 6 changes periodically, which helps to produce periodic flow rate changes in the channel. At the position where the diameter decreases, the flow rate will increase due to the reduction in the cross-sectional area of ​​the channel, forming a jet effect, which helps to enhance the mixing and reaction rate of the liquid. At the position where the diameter increases, the flow rate slows down, providing space for buffering and mixing for the liquid. The combined shape between the first reaction channel 61 and the second reaction channel 62 is a spindle structure 64, and 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. The height of the spindle structure 64 changes periodically. The height and width of the spindle are adjustable as follows Figure 8 As 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 in the channel. In the narrower part of the spindle, the flow rate will increase, forming a jet effect, which helps to push the liquid forward. In the wider part, the flow rate slows down, providing space for buffering and mixing for the liquid. The width and height of the spindle structure 64 increase and decrease periodically, which will produce periodic disturbances and shear forces in the channel. These disturbances and shear forces can destroy the laminar structure in the liquid and promote uniform mixing and full reaction of the liquid.

[0029] See also Figure 3-Figure 5, the first reaction channel 61 and the second reaction channel 62 are provided with a cross-overlapping structure 63 for mixing liquids at the staggered position, and the cross-overlapping structure 63 makes the first reaction channel 61 and the second reaction channel 62 partially overlap, and the channel slope 631 is arranged on the cross-overlapping structure 63. This design is mainly to enhance the mixing effect of the liquid and improve the reaction rate. In the cross-overlapping structure 63, the first reaction channel 61 and the second reaction channel 62 partially overlap, so that the two liquids can contact and mix with each other at the staggered 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-collision, forming strong turbulence and shear force, thereby enhancing the mixing effect of the liquid. 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 liquids have equal flow and flow rate at the staggered 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 of the first reaction channel 61. When the liquid passes through the channel slope 631, it crosses and offsets each other, mixes, and then separates into two streams of liquid, entering the first reaction channel 61 and the second reaction channel 62 respectively. The vertical height of the slope of the channel slope 631 is greater than half of the width of the first reaction channel 61 to ensure that the liquid can fully cross and offset when passing through the slope. If the vertical height of the slope is too small, the liquid may not be able to completely offset and mix; and if the vertical height of the slope is too large, the flow resistance of the liquid may increase and the reaction rate may be reduced. The reaction channel grooves 6 are arranged in two or more groups in a U-shape in 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 fully mix and react in the reaction channel grooves 6. The partitions 7 are fixedly installed on both sides of the reaction plate 1, and the partitions 7 are to ensure the closure and stability of the reaction channel grooves 6. The liquid outlet 2 penetrates through a single side of the reaction plate 1 and is opened on the partition 7 . 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 .

[0030] Working principle: After two or more liquids are transported into the reaction plate 1 from the first reaction liquid inlet 3 and the second reaction liquid inlet 4 by a pump or other means, they are circulated and mixed through the mixing channel 5, and then pass 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, thereby generating disturbances. This disturbance helps to enhance the mixing effect of the liquids and increase the reaction rate. In addition, since 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 conducive to guiding the flow of the liquid. 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. In the wider part, the flow rate slows down, providing space for buffering and mixing of the liquid. The spindle structure 64 reduces the resistance of the channel and ensures that the liquid can fill the entire reaction channel groove 6 and flow in the form of plug flow, thereby avoiding the occurrence of dead zones. When the liquid flows through the cross-overlapping 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, and then the two liquids cross again. Since there is partial channel overlap at the cross-overlapping structure 63, the two liquids collide and strengthen the disturbance degree, and then they are divided into two liquids. At the same time, channel slopes 631 are provided in the first reaction channel 61 and the second reaction channel 62. The channel slopes 631 can make the upper and lower layers of the first reaction channel 61 and the second reaction channel 62 interchangeable, so that the liquids cross-overlap at the cross-overlapping structure 63. The channel slopes 631 can not only lift and lower the channels, so that the upper and lower layers of the two channels are changed, but also increase the diffusion of the liquid in the vertical direction to increase the mixing effect. Furthermore, the upper and lower channel slopes 631 increase the contact area with the entire reaction plate 1 , thereby improving the heat exchange of the reaction channel groove 6 .

[0031] 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 affect the flow rate of the liquid. At the position where the diameter of the reaction channel groove 6 is reduced, the flow rate of the liquid will increase, forming a jet effect; while at the position where the diameter is increased, the flow rate slows down, providing space for buffering and mixing for the liquid. This change in flow rate can cause effects such as buffering, jetting, oscillation, and back mixing, thereby enhancing the mixing effect of the liquid. And when these two structural changes are superimposed on each other, their effects on the flow rate of the liquid will be superimposed on each other, thereby greatly improving the mixing rate of the liquid in the reaction channel groove 6.

[0032] It should be noted that, in this article, relational terms such as first and second, etc. are only used to distinguish one entity or operation from another entity or operation, and do not necessarily require or imply any such actual relationship or order between these entities or operations. Moreover, the terms "include", "comprise" or any other variants thereof are intended to cover non-exclusive inclusion, so that a process, method, article or device including a series of elements includes not only those elements, but also other elements not explicitly listed, or also includes elements inherent to such process, method, article or device. In the absence of further restrictions, the elements defined by the sentence "comprise a ..." do not exclude the existence of other identical elements in the process, method, article or device including the elements.

[0033] Although embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that various changes, modifications, substitutions and variations may be made to the embodiments without departing from the principles and spirit of the present invention, and that the scope of the present 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 staggered position and 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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