CN210906104U - Micro-reaction channel and micro-reactor - Google Patents
Micro-reaction channel and micro-reactor Download PDFInfo
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- CN210906104U CN210906104U CN201920701971.7U CN201920701971U CN210906104U CN 210906104 U CN210906104 U CN 210906104U CN 201920701971 U CN201920701971 U CN 201920701971U CN 210906104 U CN210906104 U CN 210906104U
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Abstract
The utility model discloses a micro-reaction channel relates to the chemical industry equipment field, include the intensive hybrid chamber along central symmetry axis bilateral symmetry, it sets up the mixed area that converges to strengthen the hybrid chamber export department, it cuts apart the body to have in the intensive hybrid chamber, cut apart the body with the inner wall of strengthening the hybrid chamber forms the first subchannel and the second subchannel of symmetry, first subchannel with the second subchannel for the central symmetry axis outwards extends to crossing connect again behind the import portion of strengthening the hybrid chamber the mixed area that converges. The advantages are that: the specific surface area is large and can reach one to fifty thousand meters2/m3(ii) a The fluid in the channel belongs to plug flow, and no vortex and back mixing exist; can haveThe conditions of poor and uneven mixing effect in the channel caused by the pulse of the feeding pump are effectively avoided; the pressure drop is small, and the mixing effect is good; under the same substrate area, the channel area that can arrange is big, does not have the waste region, therefore the liquid holdup is big, and the dwell time is long.
Description
Technical Field
The utility model relates to a chemical industry equipment field especially relates to a micro-reactor.
Background
The microreactor is a microreactor which is manufactured at least partially by using a micro-reaction technology or an ultra-precision machining technology, and the characteristic dimension of the internal structure (such as a flow channel) of the microreactor is between submicron and submillimeter. The microreactor has a much smaller characteristic dimension compared with conventional reaction equipment (such as a reaction kettle and a tubular reactor), which makes it have a large specific surface area, and the increase of gradients of some physical quantities is accelerated along with the reduction of the dimension, such as temperature gradients, pressure gradients, concentration gradients, density gradients and the like, which are particularly important for chemical reactions. The increase of the gradient leads to the increase of the driving force of mass transfer and heat transfer, thereby enlarging the diffusion flux per unit volume or unit area and strengthening the process of mass transfer and heat transfer. In addition, the amount of reaction reagents can be saved to a certain extent, the reaction process is safer and more reliable, and the industrial amplification can be simply and flexibly realized by increasing the number of the micro-reaction chambers, so that the continuous, efficient and safe chemical production is realized.
In a conventional microfluidic device, the shape of the adopted channels tends to be circular, so that the number of the arranged channels in the same plane is small, the liquid holdup is reduced, the residence time is influenced, a large area of flow dead zone exists between the diversion wall and the column in the device, and after the fluid flows to the column through the diversion wall, the fluid is impacted, so that a large amount of back mixing is caused, the plug flow state is damaged, and by-products can be generated in some chemical reactions.
In another prior microreactor, the reactor chamber is rectangular, and the outlet of the reactor chamber comprises a V-shaped channel with gradually narrowing width and a linear channel with equal width, the rectangular channel generates direct impact on the fluid flowing around the fluid, the moving direction of the fluid is directly changed by more than 90 degrees, the positive impact causes a great amount of energy loss, and the rectangular shape does not conform to the streamline of the fluid, and a great amount of dead zone is necessarily existed at the turning position.
The influence of the pump on the function of the microreactor is not considered in the two prior arts, because the pump usually adopted in the microreactor system is usually a high-pressure small-flow corrosion-resistant pump (such as a plunger pump, a diaphragm pump and the like), the working principle of the pump causes the oscillation of the flow velocity and the pressure pulse of the fluid, when two fluids are pumped simultaneously, the amount of the fluid entering the microreactor is easily caused to be not completely the same at each moment, and the concentration and the proportion of each fluid in different cavities in the reaction channel are different at the same moment, so that the reaction stability is influenced.
SUMMERY OF THE UTILITY MODEL
In view of the above-mentioned defects of the prior art, the technical problem to be solved in the utility model is to provide a no flow blind spot, fluid pressure and velocity of flow are stable, do not have back mixing, mix effectual reaction channel structure.
In order to achieve the above object, the utility model provides a micro-reaction channel, include the intensive hybrid chamber along central symmetry axis bilateral symmetry, it sets up the mixed area that converges to strengthen the hybrid chamber exit portion, it cuts apart the body to have in the intensive hybrid chamber, cut apart the body with the inner wall of strengthening the hybrid chamber forms the first subchannel and the second subchannel of symmetry, first subchannel with the second subchannel for the central symmetry axis outwards extends to the highest point and is higher than connect again behind the import portion of strengthening the hybrid chamber the mixed area that converges.
Further, the outlets of the first sub-channel and the second sub-channel are respectively provided with a first Venturi nozzle structure and a second Venturi nozzle structure.
Further, the first venturi nozzle structure and the second venturi nozzle structure have the same radius, the first sub-channel and the second sub-channel have the same diameter, and the ratio of the radius range to the diameter is 0.15 to 0.35.
Further, the opening angle of the divided body is 60 ° to 120 °.
Further, still include: the pulse damping pool is internally provided with a distribution body at the inlet part and a second winding fluid at the outlet part, and the first winding fluid is arranged between the distribution body and the second winding fluid;
the pulse damping pool is connected with the intensified mixing cavity.
The first fluid-surrounding body is provided with a plurality of fluid-surrounding plates which are vertically arranged at equal intervals, and the fluid-surrounding plates are in a continuous and bent corrugated structure, so that a plurality of parallel slits are formed in the reaction channel.
Further, the second winding body is circular.
Further, the outlet portion of the pulse damping reservoir is arranged in a "V" shape with an angle ranging from 60 ° to 150 °.
Furthermore, the distribution body is of three or more baffle structures arranged at equal angles, and gaps are formed among the baffles.
Furthermore, the micro-reaction channel is provided with a plurality of pulse damping pools, an inlet of the first pulse damping pool is connected with a material inlet, and a plurality of the intensified mixing cavities are sequentially connected between the two pulse damping pools.
Furthermore, a vortex street breaking sharp corner is arranged on the second surface of the dividing body.
The utility model also provides a micro-reactor, including aforementioned arbitrary little reaction channel.
Further, the micro reaction channel is processed on a substrate.
The utility model discloses replace intermittent type process with continuous process, through the channel structure's that strengthens mixing to inside continuous improvement optimization and enhancement, can increase substantially the reaction conversion rate, improve conversion, selectivity and the conversion rate etc. of product effectively, if utilize the high and even characteristics of mass transfer efficiency, can also realize the high polymer molecular weight homogeneous in high molecular polymerization. For the demand of productivity, the conventional reaction usually relies on increasing the size of the reactor to increase the yield, and the scale-up of the production of the microreactor is a method by which the number is enlarged to ensure safety.
The utility model discloses following technological effect has:
(1) has large specific surface area, canTo 10000-50000 m2/m3；
(2) The fluid in the channel belongs to plug flow, and no vortex and back mixing exist;
(3) the conditions of poor and uneven mixing effect in the channel caused by the pulse of the feeding pump can be effectively avoided;
(4) the pressure drop is small, and the mixing effect is good;
(5) under the same substrate area, the channel area that can arrange is big, does not have the waste region, therefore the liquid holdup is big, and the dwell time is long.
The conception, the specific structure and the technical effects of the present invention will be further described with reference to the accompanying drawings, so as to fully understand the objects, the features and the effects of the present invention.
Drawings
Other features, objects and advantages of the invention will become more apparent upon reading of the detailed description of non-limiting embodiments made with reference to the following drawings:
fig. 1 is a schematic structural diagram of a microreactor according to an embodiment of the present invention;
description of reference numerals: 100-a first material inlet; 101-second material inlet; 102-a material outlet; 200-a pulse damping pool; 201-a distribution body; 202-a first winding fluid; 203-a second winding fluid; 300-an intensified mixing chamber; 301-a first sub-channel; 302-a second sub-channel; 303-division body; 304-a first venturi nozzle structure; 305-a second venturi nozzle structure; 306-breaking the sharp angle of the vortex street; 307-confluence mixing zone.
Detailed Description
The technical contents of the preferred embodiments of the present invention will be more clearly understood and appreciated by referring to the drawings attached to the specification. The present invention may be embodied in many different forms of embodiments, and the scope of the invention is not limited to the embodiments described herein.
In the drawings, structurally identical elements are represented by like reference numerals, and structurally or functionally similar elements are represented by like reference numerals throughout the several views. The size and thickness of each component shown in the drawings are arbitrarily illustrated, and the present invention is not limited to the size and thickness of each component. The thickness of the components may be exaggerated where appropriate in the figures to improve clarity.
As shown in fig. 1, the present invention comprises a plurality of intensive mixing chambers 300 forming a reaction channel. Alternatively, the reaction channel may form a reaction channel group with the pulse damping pool 200, and include a pulse damping pool 200 and a plurality of intensive mixing chambers 300 connected in sequence. In this embodiment, there are 7 sets of reaction channels, and the number of the intensive mixing chambers 300 in each set is 5 to 6.
The materials enter from the inlet of the pulse damping pool 200 of the first reaction channel group, the materials usually enter into the microreactor through more than two different inlets, the outlet part of the pulse damping pool 200 is sequentially connected with a plurality of intensified mixing chambers 300 and then is communicated with the inlet of the pulse damping pool of the second reaction channel group, and after the above processes are repeated, the reacted materials flow out from the material outlet 102.
The microreactor as a whole comprises two base plates, and the reaction channels are formed by microfabrication between the two base plates, and can be formed on the base plates separately or on one side of the base plate.
The pulse damping pool 200 is in a general kettle shape in outer contour, and is not limited herein, and comprises a distribution body 201, a first fluid winding 202 and a second fluid winding 203, which are used for reducing the non-uniformity of pipeline flow, reducing the inertia loss, and relieving the defect of insufficient reaction or instability caused by the non-uniform pressure on the left side and the right side of a channel due to a pump, so that the fluid flow in a subsequent reinforced mixing cavity is more stable and uniform. Although the pulse damping pool 200 cannot play a role in forced mixing, the distribution body 201 and the corrugated winding fluid 202 are combined, so that the heterogeneous fluid can be prevented from being separated in the pulse damping pool due to insufficient mixing strength, and the phenomenon that the mixed fluid is layered can be effectively avoided.
The distribution body 201 is a baffle structure with three or more equal angles, has gaps between the baffle structures, is arranged at the inlet of the pulse damping pool 200, and is used for dividing two materials with certain pulses into three or more dispersed branches to form a multi-layer flow system with the layer thickness of tens of microns or hundreds of microns.
The flow is divided and flows to the first flow-winding body 202, and is composed of a plurality of flow-winding plates vertically arranged at equal intervals, each flow-winding plate has a continuous and curved corrugated structure, a plurality of parallel slits are formed in the reaction channel, and a plurality of branch flows which are dispersed before are dispersed again. When the fluid passes through the slit, the fluid is forced to contact and permeate with each other, the first winding fluid 202 is of a zigzag structure, the fluid in the slit is forced to change the flow direction for many times, and continuously collides with the corrugated structure to form a flow form similar to turbulent flow, so that efficient mixing is realized.
After the fluid flows through the first stream 202, the fluid contacts with a second stream 203 which is arranged at the outlet of the pulse damping pool 200 and is close to the first stream 202, and the materials are mixed again. In addition, the fluid circulation resistance at the two sides of the second winding fluid 203 is similar to the circulation resistance around the second winding fluid, so that the phenomenon that the fluid flows out along the middle position to cause short circuit at the two sides or the fluid is not uniform is avoided. The second winding 203 in this embodiment is circular.
The fluid has already finished the preliminary mixing after passing the second fluid winding 203, the flow direction has changed certain, its change is less than 90 °, and the flow direction is not centrosymmetric, in order to guarantee the fluid can be steady and even flow in the subsequent intensive mixing chamber 300, and avoid the fluid flow dead zone in the pulse damping pool 200, cause the fluid to be detained, therefore set up the terminal exit of the pulse damping pool 200 as the outlet that contracts, the exit department of the pulse damping pool 200 is set up as "V" shape, its angle is related to the flowrate, to different media, different flowrates in the reaction channel, the angle range is set up as 60 ° -150 °, preferably 100 °. A section of path with constant flow area is arranged behind the V-shaped outlet part. The fluid slowly enters the outlet with a small flow area from the area with a large flow area, is recombined, and is originally cut into a plurality of strands of fluid which are converged into one strand at the outlet and extruded out of the outlet to enter the intensified mixing cavity 300, and is subjected to forced penetration and mixing again.
The intensified mixing chamber 300 is an intensified mixing chamber with bilateral symmetry along a central symmetry axis, and a confluence mixing region 307 is provided at an outlet portion thereof. The intensified mixing cavity is provided with a partitioning body 303, a first sub-channel 301 and a second sub-channel 302 which are symmetrical with the inner wall of the intensified mixing cavity 300 are formed, and the first sub-channel 301 and the second sub-channel 302 extend outwards relative to the central symmetry axis to cross the inlet part of the intensified mixing cavity 300 and then are connected with a confluence mixing area 307.
Further, the outer contour of the intensified mixing chamber 300 is a left-right symmetrical "black peach shape", and a confluence mixing region 307 is arranged at the outlet part of the intensified mixing chamber. The interior of the intensified mixing chamber 300 includes a partition 303 having a first face opposite to the inlet portion of the intensified mixing chamber 300, with an opening angle of 60 ° to 120 °. The angular centerline of the dividing body 303 is collinear with the entrance to the intensified mixing chamber 300. The dividing body 303 and the inner wall of the intensified mixing chamber 300 form a left and right first sub-channel 301 and a second sub-channel 302 with equal diameters. The first sub-channel 301 and the second sub-channel 302 are symmetrical left and right along the central symmetry axis of the intensified mixing chamber 300, and the outer contours are both "U" shaped, the opening parts of the "U" shape are respectively towards the center of the intensified mixing chamber 300, and the highest points of the opening parts are all higher than the inlet part of the intensified mixing chamber 300. The first sub-channel 301 and the second sub-channel 302 extend in a predetermined direction and are provided with a first venturi nozzle structure 304 and a second venturi nozzle structure 305 at the channel outlet, respectively, through which the fluid passes before entering the confluence mixing zone 307.
After entering the intensified mixing chamber 300, the fluid hits the dividing body 303, is divided into two uniform streams, and undergoes two 80 ° to 100 ° flow direction turns through the first sub-channel 301 and the second sub-channel 302, and enters the first venturi nozzle structure 304 and the second venturi nozzle structure 305, respectively. The fluid pressure energy is converted into velocity energy, the diffusion length perpendicular to the flow direction is reduced by increasing the flow velocity, the effect of intensified mixing is achieved, the fluid is ejected out along the nozzle, and the two fluids are merged in a converging mixing area 307 in a V shape at the outlet part of the intensified mixing cavity 300 and then enter a second intensified mixing cavity which is connected subsequently.
Further, the ratio of the radius range of the venturi nozzle to the diameter of the sub-channel is 0.15 to 0.35, preferably 0.25, and the fluid in the range does not cause excessive flow resistance and can achieve good mixing effect.
According to the karman vortex street principle, when a steady incoming flow bypasses an object under a certain condition, two sides of the object periodically fall off to form double-row line vortices which are opposite in rotation direction and regularly arranged, and after nonlinear action, the karman vortex street is formed. When the utility model people tests the fluid, the fluid bypasses the dividing body 303 when the Reynolds number in the channel is approximately equal to 50, boundary layer separation occurs, and then a pair of unstable symmetrical vortexes with opposite rotating directions are generated; when the Reynolds number exceeds 50, the symmetric vortex continuously grows; when the reynolds number is approximately equal to 70, the pair of unstable symmetric vortices finally forms vortices which are opposite in rotation direction and fall off alternately up and down, the vortices can cause continuous backflow of fluid in a channel, and can bring negative effects to some chemical reactions which can generate side reactions once back mixing is performed, and once irregular vortices are formed, the pressure or medium concentration of left and right side sub-channels in a subsequent reinforced mixing channel is not uniform, so that the problems of unstable and uncontrollable mixing effect are easily caused; and many reactions need strict control of reaction residence time, and because of vortex formation, the residence time of fluid cannot be accurately calculated, so that the yield is influenced.
Thus, a vortex street breaking point 306 is provided on a second face of the dividing body 303, where the second face is the face opposite the outlet of the intensified mixing chamber 300. The vortex street breaking sharp corner 306 is utilized to break the motion path of the vortex, the vortex is prevented from being generated after the fluid bypasses the dividing body, the fluid keeps the original flow direction and flows out of the forced mixing cavity 300 to enter a subsequent forced mixing cavity, and the fluid flows forwards in a completely symmetrical flow shape in the channel.
Further, when the ratio of the remaining area of the pulse damping bath 200 excluding the internal structure to the area of the forced mixing chamber 300 is greater than 1.5, the fluid pulse in the forced mixing chamber 300 can be effectively reduced.
The foregoing has described in detail preferred embodiments of the present invention. It should be understood that numerous modifications and variations could be devised by those skilled in the art in light of the teachings of this invention without undue experimentation. Therefore, the technical solutions that can be obtained by a person skilled in the art through logic analysis, reasoning or limited experiments based on the prior art according to the concepts of the present invention should be within the scope of protection defined by the claims.
Claims (13)
1. A micro-reaction channel is characterized by comprising an intensified mixing cavity which is bilaterally symmetrical along a central symmetry axis, a confluence mixing area is arranged at the outlet of the intensified mixing cavity, a partition body is arranged in the intensified mixing cavity, the partition body and the inner wall of the intensified mixing cavity form a first sub-channel and a second sub-channel which are symmetrical, and the first sub-channel and the second sub-channel extend outwards relative to the central symmetry axis to cross over the inlet of the intensified mixing cavity and then are connected with the confluence mixing area.
2. The micro-channel of claim 1, wherein the outlets of the first and second sub-channels are provided with a first venturi nozzle structure and a second venturi nozzle structure, respectively.
3. The micro reaction channel of claim 2, wherein the first venturi nozzle structure and the second venturi nozzle structure have equal radii, the first sub-channel and the second sub-channel have equal diameters, and the ratio of the radius range to the diameters is 0.15 to 0.35.
4. The micro reaction channel as claimed in claim 1, wherein the opening angle of the partition body is 60 ° to 120 °.
5. The micro-channel of claim 1, further comprising: the pulse damping pool is internally provided with a distribution body at the inlet part and a second winding fluid at the outlet part, and the first winding fluid is arranged between the distribution body and the second winding fluid;
the pulse damping pool is connected with the intensified mixing cavity.
6. The micro-channel of claim 5, wherein the first fluid-surrounding structure has a plurality of fluid-surrounding plates vertically arranged at equal intervals, and the fluid-surrounding plates have a continuous and curved corrugated structure, so that a plurality of parallel slits are formed in the channel.
7. The micro-channel of claim 5, wherein the second winding is circular.
8. The micro-channel of claim 5, wherein the outlet portion of the pulse damping reservoir is disposed in a "V" shape with an angle ranging from 60 ° to 150 °.
9. The micro-channel of claim 5, wherein the distribution body has three or more baffle structures disposed at equal angles, and the baffles have gaps therebetween.
10. The micro-channel of any of claims 5 to 9, wherein the micro-channel has a plurality of the pulse damping pools, an inlet of a first pulse damping pool is connected to the material inlet, and a plurality of the intensive mixing chambers are connected between two pulse damping pools in sequence.
11. The micro-reaction channel according to any of claims 1 to 9, wherein the second surface of the partition body is provided with a vortex street breaking sharp corner.
12. A microreactor comprising the microreactor as claimed in any of claims 1 to 11.
13. The microreactor of claim 12, wherein said microreactor channels are fabricated on a substrate.
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| CN201920701971.7U CN210906104U (en) | 2019-05-16 | 2019-05-16 | Micro-reaction channel and micro-reactor |
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| CN201920701971.7U CN210906104U (en) | 2019-05-16 | 2019-05-16 | Micro-reaction channel and micro-reactor |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110090607A (en) * | 2019-05-16 | 2019-08-06 | 青岛三易安化工设备有限公司 | A kind of microreactor |
| CN112206695A (en) * | 2020-09-16 | 2021-01-12 | 复旦大学 | Multi-layer structure micro-channel mixer and fluid mixing method thereof |
| CN112915940A (en) * | 2021-02-10 | 2021-06-08 | 河北龙亿环境工程有限公司 | Microreactor, parallel high-efficiency microreactor and application of microreactor and parallel high-efficiency microreactor |
| CN113457591A (en) * | 2021-07-07 | 2021-10-01 | 化学与精细化工广东省实验室 | Micro-channel reactor |
| CN113546588A (en) * | 2021-07-14 | 2021-10-26 | 宁波九胜创新医药科技有限公司 | Microchannel reactor with anti-blocking structure |
-
2019
- 2019-05-16 CN CN201920701971.7U patent/CN210906104U/en not_active Withdrawn - After Issue
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110090607A (en) * | 2019-05-16 | 2019-08-06 | 青岛三易安化工设备有限公司 | A kind of microreactor |
| CN110090607B (en) * | 2019-05-16 | 2024-05-07 | 山东微井化工科技有限公司 | Micro-reactor |
| CN112206695A (en) * | 2020-09-16 | 2021-01-12 | 复旦大学 | Multi-layer structure micro-channel mixer and fluid mixing method thereof |
| CN112915940A (en) * | 2021-02-10 | 2021-06-08 | 河北龙亿环境工程有限公司 | Microreactor, parallel high-efficiency microreactor and application of microreactor and parallel high-efficiency microreactor |
| CN112915940B (en) * | 2021-02-10 | 2022-07-08 | 河北龙亿环境工程有限公司 | Microreactor, parallel high-efficiency microreactor and application of microreactor and parallel high-efficiency microreactor |
| CN113457591A (en) * | 2021-07-07 | 2021-10-01 | 化学与精细化工广东省实验室 | Micro-channel reactor |
| CN113457591B (en) * | 2021-07-07 | 2024-04-16 | 墨格微流科技(汕头)有限公司 | Microchannel reactor |
| CN113546588A (en) * | 2021-07-14 | 2021-10-26 | 宁波九胜创新医药科技有限公司 | Microchannel reactor with anti-blocking structure |
| CN113546588B (en) * | 2021-07-14 | 2022-09-23 | 宁波九胜创新医药科技有限公司 | Microchannel reactor with anti-blocking structure |
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Effective date of registration: 20210323 Address after: Room 305, B1 / F, Qingdao Institute of industrial technology, 17 Songyuan Road, high tech Zone, Qingdao, Shandong 266114 Patentee after: Shandong Weijing Chemical Technology Co.,Ltd. Address before: 266555 room 703, unit 1, building 5, no.1693 Wutaishan Road, Huangdao District, Qingdao City, Shandong Province Patentee before: QINGDAO SANYIAN CHEMICAL EQUIPMENT Co.,Ltd. |
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| AV01 | Patent right actively abandoned | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20200703 Effective date of abandoning: 20240507 |
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| AV01 | Patent right actively abandoned |
Granted publication date: 20200703 Effective date of abandoning: 20240507 |