CN115245800B - Conical spiral-flow type micro-reaction channel, micro-reactor and micro-reaction system - Google Patents
Conical spiral-flow type micro-reaction channel, micro-reactor and micro-reaction system Download PDFInfo
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- CN115245800B CN115245800B CN202110740369.6A CN202110740369A CN115245800B CN 115245800 B CN115245800 B CN 115245800B CN 202110740369 A CN202110740369 A CN 202110740369A CN 115245800 B CN115245800 B CN 115245800B
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0093—Microreactors, e.g. miniaturised or microfabricated reactors
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0046—Sequential or parallel reactions, e.g. for the synthesis of polypeptides or polynucleotides; Apparatus and devices for combinatorial chemistry or for making molecular arrays
Abstract
The invention discloses a conical spiral-flow type micro-reaction channel, which is of a cylindrical-circular truncated cone type spiral-flow channel structure and comprises a plurality of reaction units and tangential inlets connected with two adjacent reaction units, wherein: the reaction unit comprises a cylindrical reaction unit above and a truncated cone-shaped reaction unit formed by reducing the diameter downwards along the bottom end of the cylindrical reaction unit, wherein the lower end of the truncated cone-shaped reaction unit is connected with the tangential inlet, and the tangential inlet is communicated with the cylindrical reaction unit of the next reaction unit along the tangential direction. According to the invention, through ingenious space structure, the wall collision and the fluid collision are assisted while the fluid is continuously separated, combined and crushed, so that the high-efficiency mass transfer is finally realized, and meanwhile, the pressure drop is improved due to the large-bent angle strong wall collision phenomenon and the great reduction of the shrinkage reducing structure, thereby being beneficial to the industrialized amplification.
Description
Technical Field
The invention belongs to the technical field of microreactors, and in particular relates to a conical spiral-flow type microreaction channel, a microreactor and a microreaction system which are applied to the fields of chemical industry, medicine and the like and can enable reaction media to be fully mixed and perform physical or chemical reactions.
Background
Miniaturization has been an important trend in the development of natural science and engineering technology since the 90 s of the 20 th century, and miniature chemical equipment has been developed gradually. The micro-reactor has strong heat transfer and mass transfer capability, wide application prospect in the fields of chemistry, chemical industry, pharmacy, energy, environment and the like, and has the advantages of simple structure, no amplification effect, easy control of operation conditions, good reaction selectivity, internal safety and the like.
An important feature of microreactors, which is distinguished from other reactors, is that the chemical or physical reaction is controlled in as small a space as possible, the size of the reaction space being typically in the order of millimeters or even micrometers. Therefore, how to design very micro-sized reaction channels to realize hundreds of thousands of micro-reaction channels in a microreactor, so that the micro-reaction channels have higher efficiency and can realize larger yield, and further improve the heat transfer, mass transfer and mixing characteristics of the microreactor is a great problem facing the person skilled in the art.
In the design of microreactors, separation recombination is a typical mixed design concept, on the one hand by fluid separation breaking laminar boundaries and on the other hand by recombination fluid collisions. The design has good mixing efficiency when the flow speed is low, but the mixing efficiency is relatively weak in lifting amplitude along with the lifting of the flow speed/flow quantity, so that a flow dead zone is easily caused in a channel; meanwhile, in the process of improving the flow speed, the pressure drop of the separation recombination type mixing structure is obviously increased, and the efficiency of the reactor is further influenced.
Disclosure of Invention
The invention aims to provide a conical spiral-flow type micro-reaction channel, a micro-reactor and a micro-reaction system, which aim at overcoming the defects of the traditional separation and recombination type reactor structure, can obviously improve the mixing efficiency when the internal flow rate is improved, and basically has no flow dead zone inside the channel.
In order to achieve the above object, according to a first aspect of the present invention, there is provided a conical swirling type micro-reaction channel, the micro-reaction channel having a cylindrical-circular truncated cone type swirling channel structure, comprising a plurality of reaction units, and tangential inlets connecting adjacent two reaction units, wherein:
the reaction unit comprises a cylindrical reaction unit above and a truncated cone-shaped reaction unit formed by reducing the diameter downwards along the bottom end of the cylindrical reaction unit, wherein the lower end of the truncated cone-shaped reaction unit is connected with the tangential inlet, and the tangential inlet is communicated with the cylindrical reaction unit of the next reaction unit along the tangential direction.
According to the invention, the position of the cylindrical reaction unit where the tangential inlet communicates tangentially to the next reaction unit is located at the top of the cylindrical reaction unit.
According to the invention, the tangential inlet is an arcuate channel.
In the invention, the tangential inlets are distinguished according to the direction of entering the reaction unit, the tangential inlets comprise clockwise tangential inlets and anticlockwise tangential inlets, and the clockwise tangential inlets and anticlockwise tangential inlets are alternately arranged.
Preferably, two adjacent reaction units are staggered in the vertical direction.
According to the invention, the micro-reaction channel has a substantially extending direction which is a straight line or a curve; the extending direction of the curve comprises an S shape, a zigzag shape and a reverse shape.
In a second aspect of the present invention, there is provided a microreactor comprising a reaction plate and a microreaction channel as described above disposed within the reaction plate.
Further, the microreactor comprises a reaction plate and a plurality of rows of microreaction channels which are arranged in the reaction plate in parallel, wherein the tangential inlet at the tail ends of two adjacent rows of microreaction channels is lengthened so as to be directly communicated with the cylindrical reaction units of the adjacent row of microreaction channels to form serial connection, and the tail ends of the two outermost rows of microreaction channels are respectively connected with a material inlet and a material outlet through flow channels.
According to an alternative scheme, the micro-reactor is provided with two material inlets, a section of straight flow channel is respectively arranged between the two material inlets and the micro-reaction channel, two tangential inlets are formed in the top of the cylindrical reaction unit of the first reaction unit of the micro-reaction channel and are respectively communicated with the two tangential inlets.
Preferably, the two tangential inlets are located at opposite positions on top of the cylindrical reaction unit to allow better mixing of the two materials after they enter the cylindrical reaction unit.
According to a preferred embodiment of the invention, the material inlet and the material outlet of the microreactor are located on different two sides of the reaction plate, respectively.
A third object of the present invention is to provide a microreactor system formed by two or more microreactors as described above connected in series and/or parallel to each other.
The conical spiral-flow type micro-reaction channel, the micro-reactor and the reaction system have the following beneficial effects:
1. the invention uses the inertia force of fluid, the fluid enters a cylindrical reaction unit from a clockwise tangential inlet of a certain reaction unit, keeps flowing in a clockwise direction in the cylindrical reaction unit, enters a circular table-shaped reaction unit to continue flowing in a clockwise direction, then enters a anticlockwise tangential inlet of a next reaction unit, flows in the anticlockwise direction in the cylindrical reaction unit, then flows into the clockwise tangential inlet of the next reaction unit through the circular table-shaped reaction unit, enters the cylindrical reaction unit to keep flowing in a clockwise direction, and the fluid continuously flows without a flowing dead zone.
2. According to the invention, through ingenious space structure, the wall collision and the fluid collision are assisted while the fluid is continuously separated, combined and crushed, so that the high-efficiency mass transfer is finally realized, and meanwhile, the pressure drop is improved due to the large-bent angle strong wall collision phenomenon and the great reduction of the shrinkage reducing structure, thereby being beneficial to the industrialized amplification.
3. The invention has simple processing, and the micro-reactor can be realized by adopting the modes of mechanical processing, laser engraving or 3D printing.
4. The micro-reaction system provided by the invention can increase the reaction time or increase the flux through serially or parallelly connecting micro-reactors, thereby ensuring the requirement of industrial production.
Drawings
FIG. 1 is a schematic diagram of the structure of a conical swirling-type micro reaction channel of example 1.
FIG. 2 is a schematic diagram of the micro-reaction channel of FIG. 1.
Fig. 3 shows the orientation of the tangential inlets of two adjacent reaction units from a top view.
FIG. 4 is a schematic structural diagram of the microreactor of example 2.
FIG. 5 is a schematic structural diagram of the microreactor of example 3.
Fig. 6 shows the results of mass transfer performance comparison of example 5.
Description of the figure:
1-tangential inlet; a 2-reaction unit; 3. 3' -flow channel; 4. 4' -material inlet; 5-a material outlet; 10-reaction plate; 21-a cylindrical reaction unit; 22-a round table-shaped reaction unit.
Detailed Description
The invention will be further described with reference to the drawings and examples.
It should be noted that the following detailed description is illustrative and is intended to provide further explanation of the invention. Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs.
It is noted that the terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of exemplary embodiments according to the present invention. As used herein, the singular is also intended to include the plural unless the context clearly indicates otherwise, and furthermore, it is to be understood that the terms "comprises" and/or "comprising" when used in this specification are taken to specify the presence of stated features, steps, operations, devices, components, and/or combinations thereof.
In the present invention, terms such as "upper", "lower", "front", "rear", "vertical", "horizontal", "side", "bottom", "top", etc. refer to an orientation or a positional relationship based on that shown in the drawings, and are merely relational terms, which are used for convenience in describing structural relationships of various components or elements of the present invention, and do not denote any one of the components or elements of the present invention, but are not to be construed as limiting the present invention.
In the present invention, terms such as "connected," "connected," and the like are to be construed broadly and mean either fixedly connected or integrally connected or detachably connected; can be directly connected or indirectly connected through an intermediate medium. The specific meaning of the terms in the present invention can be determined according to circumstances by a person skilled in the relevant art or the art, and is not to be construed as limiting the present invention.
Microreactors are generally understood to mean microreactors which are manufactured at least in part by microreaction or ultraprecise processing techniques, and whose internal structures, such as flow channels, typically have feature sizes on the order of micrometers to millimeters.
The micro-reactor in the broad sense is a micro-reaction system mainly comprising one or more micro-reactors, auxiliary devices such as micro-mixing, heat exchange, separation, extraction and other auxiliary devices, micro-sensors, micro-actuators and other key components, and mainly aims at reaction.
The microreactor of the present invention may be any of the above.
In addition, the materials, media, and the like referred to in the present invention refer to materials that participate in mixing/reaction, and may be fluids.
The reaction medium/materials of the microreactor provided by the invention can be gaseous, liquid or dispersed for the physical or chemical reaction of the reactants in the channel.
As mentioned in the background art, the existing separation recombination type mixing structure has good mixing efficiency when the flow rate is low, but the mixing efficiency is relatively weak in lifting amplitude along with the lifting of the flow rate/flow quantity, and the pressure drop is obviously increased, so that a larger burden is brought to the operation of equipment.
Example 1, microreaction channel
As shown in fig. 1, the structure of the conical swirling type micro-reaction channel according to the present embodiment is shown. As shown in the figure, the micro-reaction channel of this embodiment is a cylindrical-circular truncated cone type swirl channel structure, specifically, the micro-reaction channel includes a plurality of reaction units 2, and a tangential inlet 1 connecting two adjacent reaction units 2, wherein the reaction units 2 include a cylindrical reaction unit 21 above, and a circular truncated cone type reaction unit 22 formed by reducing the diameter downwards along the bottom end of the cylindrical reaction unit 21, the lower end of the circular truncated cone type reaction unit 22 is connected with the tangential inlet 1, and the tangential inlet 1 is connected to the cylindrical reaction unit 21 of the next reaction unit 2 along the tangential direction.
Preferably, the position of the cylindrical reaction unit 21 where the tangential inlet 1 communicates tangentially to the next reaction unit 2 is located at the top of the cylindrical reaction unit 21 to maximize the flow path of the fluid through the reaction unit 2. Further, the tangential inlet 1 is an arc-shaped channel.
Further, said tangential inlet 1 comprises a clockwise tangential inlet and a counter-clockwise tangential inlet, distinguished by the direction of entry into the reaction unit 2. Preferably, the tangential inlets clockwise and anticlockwise are alternately arranged, that is, the tangential inlet 1 at the top of one reaction unit 2 is a tangential inlet clockwise (anticlockwise), and the tangential inlet 1 at the top of the next adjacent reaction unit 2 is a tangential inlet anticlockwise (clockwise), so that fluid enters the reaction units 2 tangentially in different rotation directions when flowing through the two adjacent reaction units 2, and the tangential inlets of the two adjacent reaction units are oriented as shown in the top view of fig. 3. Further, two adjacent reaction units 2 are staggered in the vertical direction.
In this embodiment, the cross-sectional area and thickness of the tangential inlet 1, the diameter and thickness of the cylindrical reaction unit 21, and the diameter and height of the upper and lower bottoms of the truncated cone-shaped reaction unit 22 may be adjusted according to the actual working conditions, and when the reaction flow needs to be increased or decreased, the size parameters of the reaction components may be increased or decreased. As will be apparent to those skilled in the art.
Fig. 2 shows the flow mixing principle of the conical swirling type micro reaction channel of the present embodiment. As shown by the arrow in the figure, the reaction material firstly enters the cylindrical reaction unit 21 through the tangential inlet 1 (clockwise or anticlockwise), and due to the inertia force of the fluid, the fluid enters the cylindrical reaction unit 21 to form rotational flow in the clockwise or anticlockwise direction, then flows into the circular table-shaped reaction unit 22, continues to flow in the clockwise or anticlockwise direction in rotational flow, then enters the tangential inlet 1 of the next reaction unit 2, flows into the cylindrical reaction unit 21 in the anticlockwise or clockwise direction, flows into the tangential inlet 1 of the next reaction unit 2 through the circular table-shaped reaction unit 22, and enters the next cylindrical reaction unit 21 in the clockwise or anticlockwise direction, and starts the flow mixing of the next period.
The flow field shown in fig. 1 is only a single row of channels, and in practical applications, the channels may be arranged in series or in parallel in groups, and densely packed on a reaction plate to form a microreactor (examples 2 and 3 will be described in detail).
Further, the general extension direction of the micro-reaction channel in this embodiment may be curved, such as S-shape, zigzag shape, etc., which are not described herein. The above-described modifications will be readily apparent to those skilled in the art based upon this disclosure and are intended to fall within the scope of this disclosure.
Example 2 microreactor and microreaction System
FIG. 4 is a schematic diagram of a microreactor using the microreaction channel of example 1. As shown in the figure, the microreactor comprises a reaction plate 10 and a plurality of rows of the microreaction channels described in embodiment 1 which are arranged in parallel in the reaction plate 10, wherein the tangential inlets 1 at the tail ends of two adjacent rows of the microreaction channels are lengthened to be directly communicated with the cylindrical reaction units 21 of the reaction units 2 of one adjacent row of the microreaction channels, so that series connection is formed, and the tail ends of two outermost rows of the microreaction channels are respectively connected with the material inlet 4 and the material outlet 5 through the flow channels 3. After entering through the inlet 4, the material enters the micro-reaction channel from the runner 3, passes through the reaction unit 2 of the last micro-reaction channel, and flows out of the material outlet 5 through the runner 3.
Preferably, the material inlet 4 and the material outlet 5 of the microreactor of this embodiment are respectively located on different two sides of the reaction plate 10.
And according to the requirements of actual working conditions, a serial or parallel mode can be adopted for increasing the residence time or improving the yield. For example, when it is necessary to increase the reaction time, two or more reaction plates 10 may be stacked to form a micro-reaction system. When the two reaction plates 10 are stacked, the material inlet 4 of the second reaction plate 10 corresponds to the material outlet 5 of the first reaction plate 10, so that the material flowing out through the first reaction plate 10 directly enters the second reaction plate 10 through the material inlet 4 of the second reaction plate 10. Similarly, when more reaction plates need to be stacked, no or less amplification is achieved in this way.
Example 3 microreactor and microreaction System
As shown in fig. 5, in the microreactor of another configuration using the microreaction channel of example 1, compared with the microreactor of example 2, the difference is that the microreactor has two material inlets 4, 4', a section of straight flow channels 3, 3' is respectively arranged between the material inlets 4, 4 'and the microreaction channel, and two tangential inlets 1, 1' are formed at the top of the cylindrical reaction unit 21 of the first reaction unit 2 of the microreaction channel, and the two flow channels 3, 3 'are respectively communicated with the two tangential inlets 1, 1'. Thus, two feeds enter the flow channels 3, 3' through two feed inlets 4, 4', respectively, and then enter the reaction unit 2 through tangential inlets 1, 1'. Preferably, the two tangential inlets 1, 1' are located at opposite positions on top of the cylindrical reaction unit 21, so that the two materials can be better mixed after entering the cylindrical reaction unit 21.
Likewise, the material inlets 4, 4' and the material outlets 5 of the microreactor of the present embodiment are preferably arranged on different two sides of the reaction plate 10.
Those skilled in the art will readily appreciate that the microreactors of the present embodiments may also be used in series or parallel to increase residence time or increase throughput. When it is desired to increase the residence time, in addition to connecting two or more reaction plates of this embodiment in series (e.g., stacked arrangement) with each other, the reaction plates of this embodiment may be connected in series with one or more microreactors of embodiment 2 to form a microreaction system. Specifically, the reaction plate of this embodiment is adopted as the reaction plate of the upper layer, the reaction plate of embodiment 2 is adopted as the lower layer, and the position of the material outlet of the upper layer reaction plate corresponds to the position of the material inlet of the lower layer reaction plate, so that the material flowing out of the upper layer reaction plate can directly flow into the reaction channel of the lower layer reaction plate through the material inlet of the lower layer reaction plate.
Example 4 mass transfer Performance comparison
The mass transfer performance of the microreactor of example 2 and a microreactor of type G1 of a company were compared under the condition that the oil-water phase ratio was 1 using a typical liquid-liquid extraction system "n-butanol-succinic acid-water" recommended by the european chemical engineers institute (EFCE) as an evaluation system, and the results are shown in fig. 6.
Experimental results show that the volume mass transfer coefficient of the microreactor is integrally superior to that of a G1 microreactor of a certain company within the residence time of 2-30s, and the excellent mass transfer performance of the microreactor is shown.
The above description is only of the preferred embodiments of the present invention and is not intended to limit the present invention, but various modifications and variations can be made to the present invention by those skilled in the art. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
While the foregoing description of the embodiments of the present invention has been presented in conjunction with the drawings, it should be understood that it is not intended to limit the scope of the invention, but rather, it is intended to cover all modifications or variations within the scope of the invention as defined by the claims of the present invention.
Claims (11)
1. The utility model provides a toper spiral-flow type micro-reaction channel, its characterized in that, micro-reaction channel is cylinder-round platform formula whirl channel structure, including a plurality of reaction unit to and connect the tangential import of two adjacent reaction units, wherein:
the reaction unit comprises a cylindrical reaction unit above and a truncated cone-shaped reaction unit formed by reducing the diameter downwards along the bottom end of the cylindrical reaction unit, wherein the lower end of the truncated cone-shaped reaction unit is connected with the tangential inlet, and the tangential inlet is communicated with the cylindrical reaction unit of the next reaction unit along the tangential direction;
the position of the cylindrical reaction unit, which is communicated with the next reaction unit along the tangential direction, is positioned at the top of the cylindrical reaction unit;
the tangential inlets comprise clockwise tangential inlets and anticlockwise tangential inlets, and the clockwise tangential inlets and anticlockwise tangential inlets are alternately arranged according to the direction of entering the reaction unit.
2. The micro-reaction channel of claim 1, wherein the tangential inlet is an arcuate channel.
3. The micro-reaction channel according to claim 1, wherein two adjacent reaction units are staggered in a vertical direction.
4. The micro-reaction channel according to claim 1, wherein the substantially extending direction of the micro-reaction channel is a straight line or a curved line.
5. The micro-reaction channel according to claim 4, wherein the extending direction of the curve comprises an S shape, a zigzag shape, and a zigzag shape.
6. A microreactor comprising a reaction plate and a microreaction channel disposed within the reaction plate, wherein the microreaction channel is the microreaction channel of any one of claims 1-5.
7. The micro-reactor according to claim 6, wherein the micro-reactor comprises a reaction plate and a plurality of rows of micro-reaction channels arranged in parallel in the reaction plate, wherein the tangential inlets at the tail ends of two adjacent rows of micro-reaction channels are lengthened to directly connect to the cylindrical reaction units of the reaction units of one adjacent row of micro-reaction channels, so as to form a series connection, and the tail ends of the two outermost rows of micro-reaction channels are respectively connected with a material inlet and a material outlet through flow channels.
8. The micro-reactor according to claim 7, wherein the micro-reactor is provided with two material inlets, a section of straight flow channel is respectively arranged between the two material inlets and the micro-reaction channel, two tangential inlets are formed at the top of the cylindrical reaction unit of the first reaction unit of the micro-reaction channel, and the two flow channels are respectively communicated with the two tangential inlets.
9. The microreactor of claim 8, wherein said two tangential inlets are located at opposite positions on top of a cylindrical reaction unit.
10. The microreactor according to claim 7 or 8, wherein the material inlet and the material outlet of the microreactor are located on different two sides of the reaction plate.
11. Microreactor system, characterized in that it is formed by two or more microreactors according to any one of claims 6 to 10 being connected in series and/or in parallel with each other.
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