CN116272735B - Single-layer stepped mixed reaction channel plate and micro-channel reactor - Google Patents
Single-layer stepped mixed reaction channel plate and micro-channel reactor Download PDFInfo
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- CN116272735B CN116272735B CN202310299732.4A CN202310299732A CN116272735B CN 116272735 B CN116272735 B CN 116272735B CN 202310299732 A CN202310299732 A CN 202310299732A CN 116272735 B CN116272735 B CN 116272735B
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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
- B01J19/0006—Controlling or regulating processes
- B01J19/0013—Controlling the temperature of the process
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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
- B01J19/0053—Details of the reactor
Abstract
The invention relates to the field of microreactors, and discloses a single-layer stepped mixed reaction channel plate and a microchannel reactor. The front of the channel plate body of the single-layer ladder type mixed reaction channel plate is provided with: a first fluid channel inlet; a first fluid pre-cooling/heating channel in communication with the first fluid channel inlet; a second fluid passageway inlet; a second fluid pre-cooling/heating channel in communication with the second fluid channel inlet; the fluid mixing reaction channel is provided with a plurality of ladder concave cavities which are alternately arranged along the flow direction; a reaction channel outlet communicated with the tail end of the fluid mixing reaction channel; a heat exchange liquid inlet; and a heat exchange liquid outlet. The micro-channel reactor containing the single-layer stepped mixing reaction channel plate can reduce pressure drop and improve mixing effect, so that the micro-channel reactor has wider practical application scene and is convenient for industrialized amplification.
Description
Technical Field
The invention relates to the field of microreactors, in particular to a single-layer stepped mixed reaction channel plate and a microchannel reactor.
Background
A microchannel reactor is a three-dimensional structural element that can be used to carry out chemical reactions, fabricated in a solid matrix by means of special micromachining techniques. Microchannel reactors typically contain small channel sizes and channel diversity, fluid flow in these channels, and require the desired reactions to occur in these channels. The micro-channel reactor has very large specific surface area in micro-structured chemical equipment, and has better heat and mass transfer capability than a reaction kettle.
At the microscale, the fluids exhibit a laminar flow regime in the microchannel due to the low reynolds number, i.e. two or more fluids move slowly in parallel directions and mix only by molecular diffusion. This mixing is inefficient and requires a long time and distance to achieve uniform mixing. To increase mixing efficiency, passive or active micromixers may be employed to enhance convection or turbulence between fluids. Passive micromixers refer to increasing the contact area or generating secondary flows by changing the geometry or surface properties of the channels. For example, a structure such as a partition, fold, serpentine, fishbone, etc. is provided in the channel to break the laminar flow regime. Active micromixers refer to the excitation of droplets or bubbles to produce oscillations or movements by the application of external force fields such as acoustic waves, electric fields, magnetic fields, etc. For example, piezoelectric ceramic sensors are integrated in the channels to generate ultrasonic waves that cause the droplets to oscillate.
Either passive or active micromixers result in an increase in pressure drop. As the channel cross-section changes, the velocity and pressure will also change accordingly, according to the continuity equation and bernoulli equation. Thus, in channels with complex geometries or surface features, the speed and pressure also fluctuate widely due to the frequent and intense variation of the cross section, and generally exhibit a decreasing trend along the path. This results in a higher inlet pressure to the overall system to maintain the desired mass flow. Therefore, it is necessary to consider the trade-off relationship between pressure drop and heat exchange efficiency in designing the microchannel mixing structure and select an optimization scheme according to the specific application.
In the prior art, in order to improve the mixing effect when designing the mixing unit structure of the micro-channel, for example, CN 110652949a, an eight diagrams fish-shaped reaction chamber is designed, and through continuous injection and segmentation, the structure can greatly increase the pressure of the system, and meanwhile, the practical application scenario of the micro-channel reactor is limited. For example, in the prior art, there is a type of two-phase mixing reaction, where the reaction time is 1-20 minutes, where a microreactor is required to mix continuously and efficiently, and where a lower pressure drop is required due to the longer reaction time.
In summary, it is currently difficult for microchannel reactors to achieve both excellent mixing and low pressure drop.
Disclosure of Invention
In order to solve the technical problems, the invention provides a single-layer stepped micro-channel reactor. The single-layer ladder-type micro-channel reactor can reduce pressure drop and improve mixing effect, so that the single-layer ladder-type micro-channel reactor has wider actual application scene and is convenient for industrialized amplification.
The specific technical scheme of the invention is as follows:
in a first aspect, the present invention provides a single-layer stepped mixed reaction channel plate, including a channel plate body, wherein the front surface of the channel plate body is provided with:
a first fluid channel inlet;
a first fluid pre-cooling/heating channel in communication with the first fluid channel inlet;
a second fluid passageway inlet;
a second fluid pre-cooling/heating channel in communication with the second fluid channel inlet;
the fluid mixing reaction channel is communicated with the fluid mixing reaction channel after the tail end of the first fluid pre-cooling/heating channel and the tail end of the second fluid pre-cooling/heating channel are converged, and a plurality of step concave cavities are alternately arranged on the bottom surface of the fluid mixing reaction channel along the flow direction;
a reaction channel outlet communicated with the tail end of the fluid mixing reaction channel;
a heat exchange liquid inlet;
and a heat exchange liquid outlet.
The working principle of the single-layer ladder type mixed reaction channel plate of the invention is as follows: after entering a single-layer stepped mixed reaction channel plate, the two fluids respectively pass through a pre-cooling/heating channel to preheat/cool the materials, so that the materials reach the reaction temperature before mixing; when the fluid reaches the tail end of the pre-cooling/heating channel, two fluids are converged and enter the fluid mixing reaction channel, the fluid mixing reaction channel structure adopts a special ladder-shaped design, the fluid can generate fluctuation movement when passing through the structure, the disturbance is greatly enhanced on the premise of not increasing the fluid resistance, the advection is changed into turbulent flow, and the mixing effect is enhanced.
Compared with the conventional design that the turbulence block is designed on the same horizontal plane of the flow channel to enable the fluid to realize turbulence, the stepped structure formed by the invention has the following advantages: (1) the stepped structure can change the flow direction and speed distribution of fluid effectively and increase the relative motion between fluid and the wall surface of the channel, so as to raise the mass transfer and heat transfer efficiency. (2) The ladder structure can reduce the shielding of the conventional spoiler on the cross section of the channel, and reduce the pressure loss and the energy consumption. (3) The ladder structure can utilize centrifugal force and inertia force generated by the fluctuation movement to form local vortex and secondary flow at the ladder junction, so that the turbulence degree and the turbulence intensity are further enhanced. In summary, the stepped structure not only can effectively improve the mixed heat transfer effect in the fluid channel, but also does not reduce the pressure drop compared with the conventional spoiler.
As one of the preferable schemes, the ladder concave cavities are staggered in a single row along the flow direction, two adjacent ladder concave cavities in front and back are respectively connected with different side walls of the fluid mixing reaction channel, and the included angle between the length direction of each ladder concave cavity and the side wall connected with the ladder concave cavity is 40-50 degrees.
The included angle between the length direction of the single stepped concave cavity and the side wall connected with the single stepped concave cavity is reduced, so that the pressure loss can be reduced, and the mixing efficiency of the fluid is improved. The angle between the length direction of the single stepped cavity and the side wall connected with the single stepped cavity influences the micro-mixing effect of the fluid in the micro-channel, and the mixing performance and pressure drop of the fluid in the stepped cavity can be balanced by selecting an angle of 40-50 degrees.
Further, the depth of the fluid mixing reaction channel is 0.5-1mm; the depth of the stepped concave cavity relative to the fluid mixing reaction channel is 0.2-0.6mm.
The channel depth of a microchannel reactor is an important parameter affecting fluid flow and mass transfer and generally needs to be determined according to the design goals and operating conditions of the reactor. In general, the smaller the channel depth, the smaller the Reynolds number of the fluid, the more laminar the flow tends to be; the greater the depth, the better the mass transfer efficiency and reaction rate, but too great a channel depth also increases the fluid residence time distribution and increases the difficulty of device fabrication. Therefore, when determining the channel depth of the microchannel reactor, the factors such as fluid mechanics, heat and mass transfer, chemical reaction and the like need to be comprehensively considered, and optimization is carried out by methods such as theoretical analysis, numerical simulation or experimental test.
In one embodiment, the stepped recess is important with respect to the depth of the fluid mixing reaction channel. If the flow disturbance capacity is relatively too deep, the flow disturbance capacity becomes weak, and the RTD value (residence time distribution) becomes large; if the disturbance force is too shallow, the effect cannot be achieved, the step structure with reasonable design can utilize the centrifugal force and the inertia force generated by the fluctuation motion to form local vortex and secondary flow at the step junction, and the turbulence degree and the turbulence intensity are further enhanced.
Still further, the depth of the fluid mixing reaction channel is 0.7-0.9mm; the depth of the stepped concave cavity relative to the fluid mixing reaction channel is 0.25-0.4mm.
As a second preferred scheme, the step concave cavities are divided into a shallow step concave cavity and a deep step concave cavity, and are staggered in a double row along the flow direction, and comprise a left step single row and a right step single row which are parallel to each other; the step cavities in the left step single row and the right step single row are connected with different side walls of the fluid mixing reaction channel, all the step cavities in the parallel double rows formed by the two single rows are arranged with 'shallow step cavity of the left step single row → deep step cavity of the right step single row → shallow step cavity of the right step single row → deep step cavity of the left step single row' as the minimum repeating unit along the flow direction, the left step single row is connected with the end parts of the two corresponding step cavities in the right step single row, and the included angle between the length direction of the single step cavity and the side wall connected with the single step cavity is 40-50 degrees. Compared with the scheme I, the scheme II has the advantages of more complex structure, increased processing difficulty and better effect. In the scheme II, a second-order step is arranged, when fluid flows into the step I, the fluid can flow at two sides simultaneously, the inertia force of transverse flow is increased, one side of the fluid is disturbed upwards to enter the main channel, the other side of the fluid enters the step II downwards, and meanwhile, the fluid in the other part of the main channel directly enters the step II. The two steps can make the fluid move up and down between the platforms with different heights, so as to change the speed, pressure and turbulence degree of the fluid. Compared with a ladder structure, the two-step structure has the following advantages: (1) the mixing efficiency of the fluid can be increased, and the heat transfer and mass transfer performance can be improved. (2) The impact force of the fluid on the wall surface can be reduced, and noise and vibration are reduced. (3) The distribution and direction of the fluid can be regulated, and the control of multiphase flow or non-uniform flow is realized. In addition, according to the theory of fluid mechanics, the two step structure of height can influence fluid motion through the following mechanism: (1) The step gap generates a local acceleration effect, so that a differential pressure drive is formed between the upper and lower layers of platforms. (2) A shearing effect is created at the step edge, so that a speed difference is created between the adhesive layer close to the wall and the non-adhesive layer away from the wall. (3) The vortex effect is generated at the rear of the step, so that circulation exchange is formed between a low-pressure area inside the vortex core and a high-pressure area outside the vortex.
Further, the depth of the fluid mixing reaction channel is 0.5-1mm; the depth of the shallow step concave cavity relative to the fluid mixing reaction channel is 0.1-0.3mm; the depth of the deep stepped concave cavity relative to the fluid mixing reaction channel is 0.4-0.8mm.
The two step structures of the step structure in the second scheme can enable the fluid to generate shearing and diffusion when passing through the steps, so that the uniformity and the reaction efficiency of the fluid are improved. The depth design of the high-low step structure needs to consider factors such as the Reynolds number of the fluid, pressure drop loss and the like, and is generally optimized by adopting numerical simulation or experimental test and other methods. The invention uses the Navie-Stokes equation and the continuity equation to describe the motion state of the fluid in the high-low step structure, and solves the parameters such as the velocity field, the pressure field, the temperature field and the like.
Still further, the depth of the fluid mixing reaction channel is 0.7-0.8mm; the depth of the shallow step concave cavity relative to the fluid mixing reaction channel is 0.23-0.27mm; the depth of the deep stepped concave cavity relative to the fluid mixing reaction channel is 0.45-0.55mm.
Preferably, the width of the fluid mixing reaction channel is 0.5-3mm, and further 1-2mm.
Preferably, the width of the flow passage at the junction between the first fluid pre-cooling/heating channel, the second fluid pre-cooling/heating channel and the fluid mixing reaction channel is in a reduced diameter shape. Further preferably, the included angle between the first fluid pre-cooling/heating channel and the second fluid pre-cooling/heating channel is 55-65 degrees, and the included angle between the fluid mixing reaction channel and the other two channels is equal.
In the invention, the confluence part of the first fluid pre-cooling/heating channel, the second fluid pre-cooling/heating channel and the fluid mixing reaction channel is Y-shaped. The design has the advantages that: the flow channel is designed by combining simulation effects, so that the mixing is efficient, and excessive pressure drop cannot be generated. The mixing efficiency of the common collision or the Y-shaped inlet is insufficient, the diameter reduction mode is adopted, the pressure drop is overlarge when the diameter reduction collision is carried out, and the diameter reduction mode is combined with the Y-shaped inlet, so that the flow speed enhancing mixing effect is improved, and the overlarge pressure drop can be controlled.
When the fluid reaches the tail end of the pre-cooling/heating channel, the two fluids are converged and enter the fluid mixing reaction channel, and the converging part adopts a Y-shaped reducing collision design, so that the linear speed and the collision force of the fluid can be increased instantaneously, and the pre-mixing effect of the fluid is greatly improved.
Preferably, the flow directions of the first fluid pre-cooling/heating channel, the second fluid pre-cooling/heating channel and the fluid mixing reaction channel are in a zigzag shape.
Preferably, the back surface of the channel plate body is provided with a heat exchange channel, a heat exchange liquid inlet and a heat exchange liquid outlet which are in a zigzag and roundabout shape, and a plurality of guide strips are distributed on the bottom surface of the heat exchange channel along the flow direction; two ends of the heat exchange channel are respectively communicated with the heat exchange liquid inlet and the heat exchange liquid outlet.
The heat exchange channel is designed to be matched with the heat exchange channel plate, so that heat exchange on the front side and the back side of the channel plate body can be realized, and the efficiency is higher.
In a second aspect, the invention provides a microchannel reactor comprising the following components stacked in sequence:
an upper cover plate;
the back surface of the channel plate body faces the upper cover plate;
the heat exchange channel plate, the heat exchange channel plate is equipped with the heat exchange channel taking the form of tortuous and roundabout on the surface facing away from single-layer ladder-type mixing reaction channel plate, the bottom surface of the said heat exchange channel has several guide strips along the flow direction;
and a lower cover plate.
The working principle of the microchannel reactor of the invention is as follows: the two fluids respectively enter a single-layer stepped mixed reaction channel plate, and firstly, the two fluids respectively pass through a pre-cooling/heating channel to preheat/cool materials, so that the materials reach the reaction temperature before being mixed; when the two fluids reach the tail end of the pre-cooling/heating channel of the fluid, the two fluids are converged and enter the fluid mixing reaction channel, meanwhile, the heat exchange liquid circularly flows in the heat exchange channel of the heat exchange channel plate and exchanges heat with the materials in the single-layer stepped mixing reaction channel plate, so that the materials are fully mixed and react in the flowing process of the fluid mixing reaction channel, and finally flow out of the outlet of the reaction channel.
Preferably, the upper cover plate is provided with a first fluid channel inlet, a second fluid channel inlet, a reaction channel outlet, a heat exchange liquid inlet and a heat exchange liquid outlet.
Compared with the prior art, the invention has the beneficial effects that:
(1) The micro-channel of the fluid mixing reaction channel adopts a special ladder-type design, so that fluid can generate fluctuation motion when passing through the structure, disturbance is greatly enhanced on the premise of not increasing fluid resistance, advection is changed into turbulence, and mixing effect is enhanced.
(2) The invention adopts the Y-shaped reducing collision design at the junction of the two streams after preheating/precooling, can instantaneously increase the linear speed and collision force of the streams, and greatly improves the premixing effect of the streams.
Drawings
FIG. 1 is a schematic view of a front side of a microchannel reactor according to the invention;
FIG. 2 is a schematic view of a resolution of the reverse side of a microchannel reactor of the invention;
FIG. 3 is a schematic overall view of a microchannel reactor according to the present invention;
FIG. 4 is a schematic view showing the front surface of a single-layer stepped mixed reaction channel plate according to example 1 of the present invention;
FIG. 5 is a schematic view showing the front surface of a single-layer stepped mixed reaction channel plate according to example 1 of the present invention;
FIG. 6 is a schematic illustration of a fluid mixing reaction channel comprising single row staggered step cavities according to example 1 of the present invention;
FIG. 7 is a schematic view showing the front surface of a single-layer stepped mixed reaction channel plate in example 2 of the present invention;
FIG. 8 is a schematic view showing the front surface of a single-layer stepped mixed reaction channel plate in example 2 of the present invention;
FIG. 9 is a schematic diagram of a fluid mixing reaction channel with staggered step cavities in the form of double rows according to example 2 of the present invention;
FIG. 10 is a cross-sectional view of a fluid mixing reaction channel comprising staggered step cavities in a double row configuration according to example 2 of the present invention;
FIG. 11 is a schematic view of the opposite side of a single-layer stepped mixing reaction channel plate according to the present invention;
FIG. 12 is a graph showing the results of a simulation test of a microchannel reactor according to example 1 of the invention;
FIG. 13 is a graph showing the results of a simulation test of a microchannel reactor according to example 2 of the invention.
The reference numerals are: the device comprises an upper cover plate 1, a single-layer step type mixed reaction channel plate 2, a first fluid channel inlet 21, a first fluid pre-cooling/heating channel 22, a second fluid channel inlet 23, a second fluid pre-cooling/heating channel 24, a fluid mixed reaction channel 25, a step cavity 26, a reaction channel outlet 27, a left step single column 28, a right step single column 29, a heat exchange channel plate 3, a heat exchange channel 31, a heat exchange liquid inlet 32, a heat exchange liquid outlet 33, a flow guide strip 34 and a lower cover plate 4.
Detailed Description
The invention is further described below with reference to examples.
General examples
A microchannel reactor, as shown in figures 1-3, comprising the following components, superimposed in sequence:
the upper cover plate 1 is provided with a first fluid channel inlet 21, a second fluid channel inlet 23, a reaction channel outlet 27, a heat exchange liquid inlet 32 and a heat exchange liquid outlet 33;
a single-layer stepped mixed reaction channel plate 2, wherein the back surface of the channel plate body faces the upper cover plate;
the heat exchange channel plate 3, one surface of the heat exchange channel plate facing away from the single-layer ladder-type mixed reaction channel plate is provided with a heat exchange channel 31 (two ends are respectively communicated with a heat exchange liquid inlet 32 and a heat exchange liquid outlet 33), and the bottom surface of the heat exchange channel is provided with a plurality of guide strips 34 along the flow direction;
a lower cover plate 4.
Wherein, the single-layer ladder type mixed reaction channel plate comprises a channel plate body;
the front of the channel plate body is provided with:
a first fluid passage inlet 21;
a first fluid pre-cooling/heating channel 22 in a serpentine path in communication with the first fluid channel inlet;
a second fluid passage inlet 23;
a second fluid pre-cooling/heating channel 24 in a serpentine path in communication with the second fluid channel inlet;
the fluid mixing reaction channel 25 is in a zigzag shape, the tail end of the first fluid pre-cooling/heating channel and the tail end of the second fluid pre-cooling/heating channel are converged and then are communicated with the fluid mixing reaction channel (the converging position of the three channels is in a reduced diameter shape, the included angle between the first fluid pre-cooling/heating channel and the second fluid pre-cooling/heating channel is 55-65 degrees, the included angle between the fluid mixing reaction channel and the other two channels is equal), and a plurality of stepped concave cavities 26 are staggered on the bottom surface of the fluid mixing reaction channel along the flow direction;
a reaction channel outlet 27 communicating with the end of the fluid mixing reaction channel;
a heat exchange fluid inlet 32;
a heat exchange liquid outlet 33;
as shown in fig. 11, the back surface of the channel plate body is provided with a heat exchange channel 31 in a zigzag shape, and the bottom surface of the heat exchange channel is provided with a plurality of flow guide strips 34 along the flow direction.
As one of the preferred schemes, as shown in fig. 4-6, the stepped concave cavities are staggered in a single column along the flow direction, two front and rear adjacent stepped concave cavities are respectively connected with different side walls of the fluid mixing reaction channel, and the included angle between the length direction of each stepped concave cavity and the side wall connected with the single stepped concave cavity is 40-50 degrees. In this embodiment, the depth of the fluid mixing reaction channel is 0.5 to 1mm (further preferably 0.7 to 0.9 mm) and the width is 0.5 to 3mm (further preferably 1 to 2 mm); the depth of the stepped recess relative to the fluid mixing reaction channel is 0.2-0.6mm (more preferably 0.25-0.4 mm).
As a second preferred scheme, as shown in fig. 7-10, the step cavities are divided into a shallow step cavity and a deep step cavity, and are staggered in a double row along the flow direction, and comprise a left step single row 28 and a right step single row 29 which are parallel to each other; the step cavities in the left step single column and the right step single column are connected with different side walls of the fluid mixing reaction channel, the shallow step cavities and the deep step cavities in each single column are staggered along the flow direction, all the step cavities in the parallel double columns formed by the two single columns are arranged along the flow direction by taking the minimum repeating unit of 'the shallow step cavity of the left step single column → the deep step cavity of the right step single column → the shallow step cavity of the right step single column → the deep step cavity of the left step single column', the ends of the two corresponding step cavities in the left step single column and the right step single column are connected, and the included angle between the length direction of the single step cavity and the side wall connected with the single step cavity is 40-50 degrees. In this embodiment, the depth of the fluid mixing reaction channel is 0.5 to 1mm (further preferably 0.7 to 0.8 mm) and the width is 0.5 to 3mm (further preferably 1 to 2 mm); the depth of the shallow step concave cavity relative to the fluid mixing reaction channel is 0.1-0.3mm (further preferably 0.23-0.27 mm); the depth of the deep stepped recess is 0.4-0.8mm (more preferably 0.45-0.55 mm) relative to the depth of the fluid mixing reaction channel.
Preferably, the micro-channel reactor is made of metal, glass, ceramic and the like, and is processed by machine tool carving or picosecond laser carving, the surfaces of the micro-channel reactor are polished, and diffusion welding is adopted as a whole.
Example 1
A microchannel reactor, as shown in figures 1-3, comprising the following components, superimposed in sequence:
the upper cover plate 1 is provided with a first fluid channel inlet 21, a second fluid channel inlet 23, a reaction channel outlet 27, a heat exchange liquid inlet 32 and a heat exchange liquid outlet 33;
a single-layer stepped mixed reaction channel plate 2, wherein the back surface of the channel plate body faces the upper cover plate;
the heat exchange channel plate 3, the heat exchange channel 31 (both ends are communicated with the heat exchange liquid inlet 32 and the heat exchange liquid outlet 33 respectively) which is in a zigzag and roundabout shape (5U-shaped bends are all 180 degrees) is arranged on one surface of the heat exchange channel plate facing away from the single-layer ladder-type mixed reaction channel plate, and a plurality of guide strips 34 are distributed on the bottom surface of the heat exchange channel along the flow direction;
a lower cover plate 4.
As shown in fig. 4-6, the single-layer stepped mixed reaction channel plate comprises a channel plate body;
the front of the channel plate body is provided with:
a first fluid passage inlet 21;
a first fluid pre-cooling/heating channel 22 (total length 0.8 m) in a zigzag shape (provided with 4 180 degree U-shaped bends and 2 right angle bends in turn) communicated with an inlet of the first fluid channel;
a second fluid passage inlet 23;
a second fluid pre-cooling/heating channel 24 (total length 0.8 m) in a zigzag shape (provided with 4 180 degree U-shaped bends and 1 135 degree bends in sequence) communicated with an inlet of the second fluid channel;
the fluid mixing reaction channel 25 (total length 1 m) is in a zigzag shape (6U-shaped bends of 180 degrees are sequentially arranged), the tail end of the first fluid pre-cooling/heating channel and the tail end of the second fluid pre-cooling/heating channel are converged and then are communicated with the fluid mixing reaction channel (the converging positions of the three channels are in a reducing shape, the included angle between the first fluid pre-cooling/heating channel and the second fluid pre-cooling/heating channel is 60 degrees, and the included angle between the fluid mixing reaction channel and the other two channels is 150 degrees), and in the scheme, a plurality of parallelogram-shaped stepped concave cavities 26 which are in a single-row shape and equidistantly staggered arrangement are arranged on the bottom surface of the fluid mixing reaction channel along the flow direction. Wherein, two adjacent ladder cavitys are respectively with the left and right sides wall of fluid mixing reaction passageway links up (two adjacent ladder cavitys (a left and right side) are in the front and back is 3.8mm in the central point interval in the flow direction, and single ladder cavity length in the flow direction is 2mm, and the free end of ladder cavity is 2mm with the interval of runner lateral wall), and the length direction of single ladder cavity is 45 degrees with the contained angle of the lateral wall that links up. In this embodiment, the depth of the fluid mixing reaction channel is 0.8 mm) and the width is 2mm; the depth of the stepped cavity relative to the fluid mixing reaction channel was 0.3mm.
A reaction channel outlet 27 communicating with the end of the fluid mixing reaction channel;
a heat exchange fluid inlet 32;
a heat exchange liquid outlet 33;
as shown in fig. 11, the back surface of the channel plate body is provided with heat exchange channels 31 in a zigzag shape (5U-bends of 180 degrees in total), and the bottom surfaces of the heat exchange channels are distributed with a plurality of flow guide strips 34 along the flow direction.
The micro-channel reactor is made of metal, the machining mode is machine tool engraving, the surfaces are polished, and diffusion welding is adopted integrally.
The working principle of the microchannel reactor of the embodiment is as follows: the two fluids respectively enter a single-layer stepped mixed reaction channel plate, and firstly, the two fluids respectively pass through a pre-cooling/heating channel to preheat/cool materials, so that the materials reach the reaction temperature before being mixed; when the two fluids reach the tail end of the pre-cooling/heating channel of the fluid, the two fluids are converged and enter the fluid mixing reaction channel, and meanwhile, the heat exchange liquid circularly flows in the heat exchange channel of the heat exchange channel plate and exchanges heat with the materials in the single-layer stepped mixing reaction channel plate, so that the materials are fully mixed and react in the flowing process of the fluid mixing reaction channel. The fluid mixing reaction channel micro-channel adopts a special ladder type design, fluid can generate fluctuation motion when passing through the structure, disturbance is greatly enhanced on the premise of not increasing fluid resistance, advection is changed into turbulence, and mixing effect is enhanced.
Simulation test: the microchannel reactor of example 1 was used as a fluid medium model for simulation test, and the concentration standard deviation was used as a fluid mixing effect evaluation, and as shown in FIG. 12, the mixing effect could reach 99.21%, 99.62% and 99.99% at flow rates of 1mm/s, 10mm/s and 100mm/s, respectively.
Example 2
Example 2 differs from example 1 in that: as shown in fig. 7-10, in the single-layer stepped mixed reaction channel plate, the stepped concave cavities are divided into a shallow stepped concave cavity and a deep stepped concave cavity, and are staggered in a double row form along the flow direction, and comprise a left stepped single row 28 and a right stepped single row 29 which are parallel to each other; the step cavities in the left step single column and the right step single column are connected with the left side wall and the right side wall of the fluid mixing reaction channel (all the step cavities are in a parallelogram shape and have the same size), the shallow step cavities and the deep step cavities in each single column are staggered along the flow direction, all the step cavities in the parallel double columns consisting of the left step single column and the right step single column are arranged along the flow direction by taking the 'shallow step cavity of the left step single column → deep step cavity of the right step single column → shallow step cavity of the right step single column → deep step cavity of the left step single column' as the minimum repeating unit, the left step single column is connected with the end parts of the corresponding two step cavities in the right step single column, and the included angle between the length direction of the single step cavity and the connected side wall is 45 degrees. In this embodiment, the depth of the fluid mixing reaction channel is 0.75 mm) and the width is 2mm; the depth of the shallow step concave cavity relative to the fluid mixing reaction channel is 0.25 mm); the depth of the deep stepped cavity is 0.5mm relative to the depth of the fluid mixing reaction channel. The center distance between the two adjacent ladder cavities in the front and back of the left ladder single column (left) in the flow direction is 2.8mm, and the center distance between the two adjacent ladder cavities in the left and right ladder cavities which are mutually connected in the flow direction is 1mm.
The micro-channel reactor is made of metal, the machining mode is machine tool precise engraving, the surfaces are polished, and diffusion welding is adopted integrally.
Simulation test: the micro-channel reactor of example 2 was used as a fluid medium model for simulation test, and as shown in FIG. 13, the mixing effect was 99.9% at a flow rate of 5 mm/s.
The raw materials and equipment used in the invention are common raw materials and equipment in the field unless specified otherwise; the methods used in the present invention are conventional in the art unless otherwise specified.
The foregoing description is only a preferred embodiment of the present invention, and is not intended to limit the present invention, and any simple modification, variation and equivalent transformation of the above embodiment according to the technical substance of the present invention still fall within the scope of the technical solution of the present invention.
Claims (11)
1. A single-layer stepped mixed reaction channel plate, characterized in that: including the passageway board body, the front of passageway board body is equipped with:
a first fluid channel inlet;
a first fluid pre-cooling/heating channel in communication with the first fluid channel inlet;
a second fluid passageway inlet;
a second fluid pre-cooling/heating channel in communication with the second fluid channel inlet;
the fluid mixing reaction channel is communicated with the fluid mixing reaction channel after the tail end of the first fluid pre-cooling/heating channel and the tail end of the second fluid pre-cooling/heating channel are converged, and a plurality of step concave cavities are alternately arranged on the bottom surface of the fluid mixing reaction channel along the flow direction;
a reaction channel outlet communicated with the tail end of the fluid mixing reaction channel;
the arrangement mode of the step concave cavities is as scheme one or scheme two:
scheme one: the step cavities are staggered in a single row along the flow direction, two adjacent step cavities in front and back are respectively connected with different side walls of the fluid mixing reaction channel, and the included angle between the length direction of each step cavity and the connected side wall is 40-50 degrees;
scheme II: the step concave cavities are divided into a shallow step concave cavity and a deep step concave cavity, and are staggered in a double row along the flow direction, and comprise a left step single row and a right step single row which are parallel to each other; the step cavities in the left step single row and the right step single row are connected with different side walls of the fluid mixing reaction channel, all the step cavities in the parallel double rows formed by the two single rows are arranged with 'shallow step cavity of the left step single row → deep step cavity of the right step single row → shallow step cavity of the right step single row → deep step cavity of the left step single row' as the minimum repeating unit along the flow direction, the left step single row is connected with the end parts of the two corresponding step cavities in the right step single row, and the included angle between the length direction of the single step cavity and the side wall connected with the single step cavity is 40-50 degrees.
2. The single-layer stepped mixing reaction channel plate according to claim 1, wherein: in scheme one:
the depth of the fluid mixing reaction channel is 0.5-1mm;
the depth of the stepped concave cavity relative to the fluid mixing reaction channel is 0.2-0.6mm.
3. The single-layer stepped mixing reaction channel plate according to claim 2, wherein: in scheme one:
the depth of the fluid mixing reaction channel is 0.7-0.9mm;
the depth of the stepped concave cavity relative to the fluid mixing reaction channel is 0.25-0.4mm.
4. The single-layer stepped mixing reaction channel plate according to claim 1, wherein: in the scheme II:
the depth of the fluid mixing reaction channel is 0.5-1mm;
the depth of the shallow step concave cavity relative to the fluid mixing reaction channel is 0.1-0.3mm;
the depth of the deep stepped concave cavity relative to the fluid mixing reaction channel is 0.4-0.8mm.
5. The single-layer stepped mixing reaction channel plate according to claim 4, wherein: in the scheme II:
the depth of the fluid mixing reaction channel is 0.7-0.8mm;
the depth of the shallow step concave cavity relative to the fluid mixing reaction channel is 0.23-0.27mm;
the depth of the deep stepped concave cavity relative to the fluid mixing reaction channel is 0.45-0.55mm.
6. The single-layer stepped mixing reaction channel plate according to any one of claims 1 to 5, wherein: and the width of a flow passage at the converging position among the first fluid pre-cooling/heating channel, the second fluid pre-cooling/heating channel and the fluid mixing reaction channel is in a reduced diameter shape.
7. The single-layer stepped mixing reaction channel plate according to claim 6, wherein: the included angle between the first fluid pre-cooling/heating channel and the second fluid pre-cooling/heating channel is 55-65 degrees, and the included angle between the fluid mixing reaction channel and the other two channels is equal.
8. The single-layer stepped mixing reaction channel plate according to any one of claims 1 to 5, wherein: the flow directions of the first fluid pre-cooling/heating channel, the second fluid pre-cooling/heating channel and the fluid mixing reaction channel are in a zigzag and circuitous way.
9. The single-layer stepped mixing reaction channel plate according to any one of claims 1 to 5, wherein: the back surface of the channel plate body is provided with a heat exchange channel which is in a zigzag and roundabout shape, a heat exchange liquid inlet and a heat exchange liquid outlet, and a plurality of guide strips are distributed on the bottom surface of the heat exchange channel along the flow direction; two ends of the heat exchange channel are respectively communicated with the heat exchange liquid inlet and the heat exchange liquid outlet.
10. A microchannel reactor comprising the following components stacked in sequence:
an upper cover plate;
the single-layer stepped mixing reaction channel plate according to any one of claims 1 to 9, wherein the opposite surface of the channel plate body faces the upper cover plate;
the heat exchange channel plate, the heat exchange channel plate is equipped with the heat exchange channel taking the form of tortuous and roundabout on the surface facing away from single-layer ladder-type mixing reaction channel plate, the bottom surface of the said heat exchange channel has several guide strips along the flow direction;
and a lower cover plate.
11. The microchannel reactor of claim 10, wherein: the upper cover plate is provided with a first fluid channel inlet, a second fluid channel inlet, a reaction channel outlet, a heat exchange liquid inlet and a heat exchange liquid outlet.
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