CN211886766U - Rotational flow type micro-reaction channel, substrate, reactor and system - Google Patents

Abstract

The utility model provides a rotational flow type micro-reaction channel, a substrate, a reactor and a system, which comprises an input section, an output section and a plurality of reaction mechanisms arranged between the input section and the output section, wherein each reaction mechanism comprises a first reaction unit positioned on the upper layer and a third reaction unit positioned on the lower layer; the first reaction unit comprises a first part for maintaining the rotary flow of the fluid and a second part tangentially connected with the first part; the third reaction unit has the same structure as the first reaction unit, is staggered with the first reaction unit in the vertical direction and is oppositely arranged in the horizontal direction; and the adjacent first reaction unit and the third reaction unit are communicated end to end through the second reaction unit positioned in the middle layer to form a continuous reaction channel. There is substantially no flow dead space.

Description

Rotational flow type micro-reaction channel, substrate, reactor and system

Technical Field

The utility model belongs to microchannel reactor, concretely relates to whirl formula micro reaction channel, base plate, reactor and system.

Background

The statements in this section merely provide background information related to the present disclosure and may not necessarily constitute prior art.

The micro chemical technology can be widely applied to the fields of chemistry, chemical engineering, energy, environment and the like due to the super-strong heat and mass transfer capacity, and secondary flow with the direction different from the main flow direction is caused by various changes of a channel structure in the design of the micro reactor, so that a fluid unit is subjected to a series of changes such as stretching, folding and splitting, the contact area between fluids is greatly improved, and the mass transfer efficiency is further improved. Separation and recombination are typical mixed design ideas, on one hand, laminar flow boundaries are broken through fluid separation, on the other hand, fluid collision is carried out through recombination, and at present, a mainstream microchannel structure such as an umbrella-shaped reactor belongs to the class.

However, as the inventor knows, the separation and recombination type mixing structure has good mixing efficiency when the flow rate is low, but the increase amplitude of the mixing efficiency is relatively weak along with the increase of the flow rate/flow rate, which easily causes a flow dead zone in a channel, and meanwhile, the pressure drop of the separation and recombination type mixing structure is remarkably increased in the process of increasing the flow rate, which further affects the efficiency of the reactor.

Disclosure of Invention

The utility model discloses a solve above-mentioned problem, provide a whirl formula micro reaction passageway, base plate, reactor and system, the utility model discloses compare in traditional separation heavy construction class reactor structure, the mass transfer coefficient of whirl structure when the internal flow rate more than or equal to setting value improves obviously, and the inside dead zone that does not basically have of passageway flows, is particularly useful for the pharmacy enterprise application that the dead zone required to be strict to the passageway flow.

According to some embodiments, the utility model adopts the following technical scheme:

the utility model discloses a first purpose provides a whirl formula micro-reaction channel utilizes the design of ingenious whirl structure, relies on fluidic inertia power to be used for mixing the fluid, when higher velocity of flow, has higher mixing efficiency, and does not have the dead zone of flowing.

In some embodiments, a swirling flow type micro reaction channel comprises an input section, an output section and a plurality of reaction mechanisms arranged between the input section and the output section, wherein each reaction mechanism comprises a first reaction unit positioned on an upper layer and a third reaction unit positioned on a lower layer;

the first reaction unit comprises a first part for maintaining the rotating flow of the fluid and a second part tangentially connected with the first part;

the third reaction unit has the same structure as the first reaction unit, is staggered with the first reaction unit in the vertical direction and is oppositely arranged in the horizontal direction;

and the adjacent first reaction unit and the third reaction unit are communicated end to end through the second reaction unit positioned in the middle layer to form a continuous reaction channel.

According to the design scheme, each unit is located in different layers/planes, a three-dimensional continuous flowing environment is ingeniously constructed, the reaction medium entering the three-dimensional continuous flowing environment can be guaranteed to continuously mix and flow through each unit, and finally a powerful mixing effect is achieved.

Secondly, end to end connection between each unit, and first reaction unit and third reaction unit structure are the same, and the position is crisscross to be laid, all has a first part that is used for keeping fluid rotational flow to and the second part of being connected with first part tangential, can guarantee that the medium forms rotational flow after getting into the upper strata, then the tangential gets into the lower floor, continues the rotational flow, and in cycles, rely on fluidic inertia force to act on all the time and mix the fluid, the effectual mixed effect that has improved.

In an alternative embodiment, the first member is disc-shaped. The fluid forms a rotational flow after entering the disc.

In an alternative embodiment, the second component is a connecting channel, the connecting channel is an arc-shaped channel, and the arc-shaped channel is bent towards the first component.

In an alternative embodiment, the second component is a connecting channel, the connecting channel comprises a straight channel and an arc channel, and the arc channel is bent towards the first component.

The arc-shaped channel ensures the smoothness, can effectively reduce dead zones and adapts to corresponding working conditions.

As an alternative embodiment, the first and second parts are smoothly transitioned between. The resistance action to the medium/material can be reduced as much as possible, and the dead zone is reduced.

As an alternative embodiment, the junction of the second reaction unit and the first reaction unit is disposed at the center of the first member of the first reaction unit. The fluid flow guiding device is arranged at the central position and is matched with the central position where the fluid continuously flows and migrates after flowing in a rotating manner, so that the smooth flowing of the fluid is ensured.

As an alternative embodiment, the input section is a first/third reaction unit and is provided with at least two inlets.

As an alternative embodiment, the output section is a first/third reaction unit and is provided with at least one outlet.

The second purpose of the utility model is to provide a micro-reaction substrate, which comprises a substrate body, wherein a plurality of rows of first reaction units are arranged on the substrate body, the first reaction units in the same row are arranged at intervals and have the same arrangement direction, and the first reaction units in adjacent rows are arranged oppositely;

or the substrate body is provided with the rotational flow type micro reaction channel.

As an alternative embodiment, the micro-reaction substrate is further provided with an input section or/and an output section.

Of course, there is also a substrate on which several rows of the second reaction units are disposed.

The third objective of the present invention is to provide a microreactor, which comprises a first reaction substrate, a second reaction substrate and a third reaction substrate arranged in parallel, wherein the contact surface between the first reaction substrate and the second reaction substrate is provided with an input section or/and an output section, a plurality of rows of first reaction units in the same plane, the first reaction units in the same row are arranged at intervals and have the same direction, the first reaction units in adjacent rows are arranged relatively, and each first reaction unit comprises a first component for keeping the fluid to flow in a rotating manner and a second component tangentially connected with the first component;

a plurality of rows of penetrating second reaction units are arranged on the second reaction substrate;

and a plurality of rows of third reaction units in the same plane are arranged on the contact surface of the third reaction substrate and the second reaction substrate, the third reaction units have the same structure as the first reaction units, are staggered in the vertical direction with the first reaction units, and are oppositely arranged in the horizontal direction.

Or, the reactor comprises a fourth reaction substrate provided with the swirling flow type micro reaction channel.

As a possible embodiment, a first end plate and a second end plate are further included, and the first end plate and the second end plate are respectively disposed at the outer sides of the first reaction substrate and the third reaction substrate.

Or the first end plate and the second end plate are respectively arranged at two sides of the fourth reaction substrate.

As a possible embodiment, the first reaction substrate, the second reaction substrate and the third reaction substrate are detachably connected or integrally non-detachably connected;

the first end plate and the second end plate are detachably connected with the first reaction substrate and the third reaction substrate.

Or the first end plate, the second end plate and the fourth reaction substrate are detachably connected or integrally and non-detachably connected.

As a possible embodiment, a sealing structure is provided between the first end plate and the first reaction substrate, between the first reaction substrate and the second reaction substrate, between the second reaction substrate and the third reaction substrate, and between the third reaction substrate and the second end plate.

Or sealing structures are arranged among the first end plate, the second end plate and the fourth reaction substrate.

A fourth object of the present invention is to provide a micro-reaction system, comprising a plurality of micro-reactors connected in series or in parallel.

Compared with the prior art, the beneficial effects of the utility model are that:

the utility model discloses utilize fluidic inertial force to act on, the fluid forms rotatory flow after getting into first part, finally reachs central point through outer continuous flow migration and puts, and the fluid gets into the lower floor through the second reaction unit, then inside the tangential gets into the first part of lower floor, the continuous flow of fluid does not have the dead zone that flows.

The utility model discloses an ingenious space structure, when the continuous separation combination of fluid is broken, supplementary with the wall collision, the high-efficient mass transfer of final realization is collided to the fluid, simultaneously, because the strong wall striking of big bent angle and the significantly reduced who reduces reducing structure, pressure drop has also obtained the improvement, does benefit to the industrialization and enlargies.

The utility model discloses processing is simple, and the reaction substrate can take the laser sculpture mode to realize.

The utility model provides a reaction system can increase the reaction time or increase flux through the series-parallel connection micro-reactor, guarantees industrial production's demand.

Drawings

The accompanying drawings, which form a part of the specification, are included to provide a further understanding of the invention, and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the invention without unduly limiting the scope of the invention.

FIG. 1(a) is a schematic view of an upper channel in accordance with the first embodiment;

FIG. 1(b) is a schematic diagram of a middle layer channel according to the first embodiment;

FIG. 1(c) is a schematic view of the lower channel of the first embodiment;

FIG. 2 is a schematic view of a reaction mechanism formed in accordance with the first embodiment;

FIG. 3 is a schematic view of a reaction channel formed in accordance with one embodiment;

FIG. 4 is a schematic view illustrating a flow process of a fluid according to an embodiment;

FIG. 5 is a schematic view of the reactor installation of the second embodiment;

FIG. 6 is a three-dimensional view of the reactor of example two;

FIG. 7(a) is a structural view of an upper reaction plate of the reactor in the second example;

FIG. 7(b) is a structural view of a middle layer reaction plate of the reactor in the second example;

FIG. 7(c) is a view showing the structure of the lower reaction plate of the reactor in the second example;

FIG. 8 is a simulated velocity cloud;

FIG. 9 is a graph showing the results of a volumetric mass transfer coefficient test.

Wherein: 1. a disc channel; 2. a connecting channel 3 and an outlet; 4. an upper mixing channel; 5. an aperture; 6. a lower layer mixing channel; 7. an upper end plate; 8. an upper reaction plate; 9. an intermediate reaction plate; 10. a lower reaction plate; 11. a lower end plate.

The specific implementation mode is as follows:

the present invention will be further explained with reference to the accompanying drawings and examples.

It should be noted that the following detailed description is exemplary 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 example embodiments in accordance with the invention. As used herein, the singular forms "a", "an" and "the" are intended to include the plural forms as well, and it should be understood that when the terms "comprises" and/or "comprising" are used in this specification, they specify the presence of stated features, steps, operations, devices, components, and/or combinations thereof, unless the context clearly indicates otherwise.

In the present invention, the terms such as "upper", "lower", "left", "right", "front", "rear", "vertical", "horizontal", "side", "bottom", and the like indicate the position or positional relationship based on the position or positional relationship shown in the drawings, and are only the terms determined for convenience of describing the structural relationship of each component or element of the present invention, and are not specific to any component or element of the present invention, and are not to be construed as limiting the present invention.

In the present invention, terms such as "fixedly connected", "connected", and the like are to be understood in a broad sense, and may be fixedly connected, or may be integrally connected or detachably connected; may be directly connected or indirectly connected through an intermediate. The meaning of the above terms in the present invention can be determined according to specific situations by persons skilled in the art, and should not be construed as limiting the present invention.

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 an internal structure (such as a flow channel) of the microreactor is generally between submicron and millimeter.

The micro-reactor in the broad sense refers to a micro-reaction system which mainly aims at reaction, mainly comprises one or more micro-reactors, and also can comprise auxiliary devices such as micro-mixing, heat exchange, separation and extraction, and key components such as micro-sensors and micro-actuators.

The microreactor of the present invention may be any of those described above.

In addition, the materials, media and the like in the present invention refer to the materials participating in the mixing/reaction, and may be fluids.

The reaction medium/material of the microreactor provided by the utility model can be gaseous, liquid or dispersed, and is used for the reactants to carry out physical reaction or chemical reaction in the channel.

As mentioned in the background, the existing separation and recombination type mixing structure has good mixing efficiency at low flow rate, but the increase amplitude of the mixing efficiency is relatively weak along with the increase of the flow rate, and the pressure drop is remarkably increased, which brings great burden to the operation of the equipment.

The first embodiment is as follows: in order to solve the above problems, a multilayer channel structure is proposed. In the present embodiment, the three-layer channel structure is shown in fig. 2, and includes an upper-layer mixing channel 4, a middle-layer mixing channel, and a lower-layer mixing channel 6.

As shown in fig. 1(a), the upper mixing channel 4 includes a plurality of first reaction units (solid line plus black area), each of which is composed of a connecting channel 2 tangentially connecting with a disc channel 1. Wherein, the connecting channel 2 is an arc channel or an approximate arc channel, one end is tangentially connected with the disc channel 1, and the other end is provided with a bend facing the disc channel 1.

And each part of the connecting channel 2 is smoothly or roundly arranged, including the connection with the disc channel 1, and the other end. So as to effectively reduce the resistance and reduce the flow dead zone.

In the present embodiment, the connecting channel 2 is a uniform cross-section channel. The cross-sectional shape includes but is not limited to rectangular, circular, or elliptical, etc.

Of course, unequal cross-sections are also possible.

Meanwhile, a certain distance is arranged between every two first reaction units, and the distance is that the lengths of the first reaction units are basically the same.

As shown in fig. 1(c), each reaction unit (or becomes a mixing unit) of the lower mixing channel 6 (solid line plus black area) is composed of the connecting channel 2 tangentially connecting with the disk channel 1, similarly to the first reaction unit of the upper mixing channel 4.

Each reaction unit (referred to as a third reaction unit for convenience of distinction) of the lower-layer mixing channel 6 is arranged in a direction opposite to that of the first reaction unit, i.e., is rotated by a certain angle along a horizontal axis (in the present embodiment, some are about 180 °, some are about 270 °, and of course, other angles may be provided according to different channel layouts). Are also spaced apart from each other. The rest of the parts corresponding to the first reaction unit will not be described in detail herein.

As shown in fig. 1(b), the reaction unit of the intermediate mixing channel (referred to as a second reaction unit) (solid line plus black area) has a hole 5 structure, each reaction unit is located at the center of the disc channel 1 of the corresponding first reaction unit or third reaction unit, and may also be referred to as an intermediate hole 5 structure.

The upper and lower layer mixing channels are connected by a middle hole 5 of the middle mixing channel, the main flow mixing principle is shown in fig. 3 and fig. 4, the material in the reaction chamber A, B firstly enters the first reaction unit of the upper layer from the inlet shown in fig. 3, the fluid forms a rotary flow after entering the disc channel 1 due to the inertia force action of the fluid, the fluid continuously flows and migrates through the outer layer of the disc channel 1 and finally reaches the central position of the disc channel 1, the fluid enters the connecting channel 2 of the third reaction unit of the lower layer through the middle hole 5 of the middle layer mixing channel, then tangentially enters the disc channel 1 of the other third reaction unit of the lower layer mixing channel 6, the fluid continuously flows, and then enters the connecting channel 2 of the other first reaction unit of the upper layer through the middle hole 5 of the middle layer mixing channel to start the flow mixing of the next period. Until it exits through the outlet 3.

In the first embodiment, the fluid region shown in fig. 1 is only a single row of channels, and in practical applications, the channels may be densely distributed on the channel plate in a continuous series manner or in a grouped parallel manner.

That is, in other embodiments, the general extending direction of the reaction channel may not be a straight line, but a curve, such as S-shape, zigzag, etc., which will not be described herein. However, the above modifications are easily conceivable for those skilled in the art based on the present application, and should fall within the protection scope of the present invention.

In order to ensure the sealing property, the width of the connecting channel 2 is the same as the diameter of the second reaction unit, and one end of the connecting channel 2 should be matched with the shape of the hole 5 of the second reaction unit.

Meanwhile, the connection position of the second reaction unit and the disk channel 1 of the first reaction unit should be as central as possible in the disk channel 1.

The channel structure can be realized by adopting the reaction plate of the second embodiment.

In the second embodiment, five reaction plates, i.e., an upper end plate 7, an upper layer reaction plate 8, a middle reaction plate 9, a lower layer reaction plate 10, and a lower end plate 11, are provided, and are connected by peripheral bolts to form a closed whole, and mirror sealing or sealing ring sealing is adopted between the plates, which is the same as the conventional assembly method and is not repeated. The installation of the respective channel plates is shown in fig. 5 and 6.

The upper end plate 7 is a cover on the apparatus for sealing with the upper reaction channel and provides two inlets for the AB reactant material into the upper reaction plate 8, as shown in fig. 7 (a). Meanwhile, the back of the layer structure can be designed with heat exchange channels similar to other conventional reaction channels, and details are not repeated here.

The inner side of the upper reaction plate 8 provides an upper mixing reaction channel, and two materials entering through the upper cover plate enter the reaction channel.

The middle reaction plate, as shown in FIG. 7(b), is provided on the inner side with a through channel connecting the upper and lower disk channels 1, through which the fluid is shuttled between the upper and lower reaction plates.

The lower reaction plate 10, as shown in FIG. 7(c), provides a lower mixing reaction channel on the inner side.

All the reaction units are connected end to end in sequence, but the adjacent reaction units are not in the same plane, so that a spatial three-dimensional structure is formed.

Of course, in other embodiments, the multilayer mixing channel structure of the first embodiment can also be fabricated on a reaction substrate.

EXAMPLE III

A reaction system can adopt a serial or parallel mode according to actual working conditions, and is used for increasing residence time or improving yield without amplification effect.

In the above embodiment, no flow dead zone exists in the structured mixing channel, as shown in fig. 8, a velocity vector diagram obtained by CFD software calculation has no flow dead zone in the channel and high mass transfer efficiency, and fig. 9 is a comparison of a small-scale rotational flow structure obtained by an extraction experiment and the mass transfer coefficient of a small-scale umbrella-shaped structure of the company before, it can be seen that the mass transfer coefficient does not decrease after the rotational flow structure channel is enlarged, and is equivalent to the mass transfer coefficient of an umbrella-shaped mixer structure with a liquid holdup of only 0.92m l.

The mass transfer efficiency is obviously improved along with the flow velocity, and after the channel is properly amplified, the amplification effect on the mass transfer does not exist as long as the same flowing Reynolds number is ensured.

The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.

Although the present invention has been described with reference to the accompanying drawings, it is not intended to limit the scope of the present invention, and those skilled in the art should understand that various modifications or variations that can be made by those skilled in the art without inventive work are still within the scope of the present invention.

Claims (10)

1. A swirl type micro-reaction channel is characterized in that: the device comprises an input section, an output section and a plurality of reaction mechanisms arranged between the input section and the output section, wherein each reaction mechanism comprises a first reaction unit positioned on the upper layer and a third reaction unit positioned on the lower layer;

the first reaction unit comprises a first part for maintaining the rotating flow of the fluid and a second part tangentially connected with the first part;

the third reaction unit has the same structure as the first reaction unit, is staggered with the first reaction unit in the vertical direction and is oppositely arranged in the horizontal direction;

and the adjacent first reaction unit and the third reaction unit are communicated end to end through the second reaction unit positioned in the middle layer to form a continuous reaction channel.

2. A cyclonic micro reaction channel as claimed in claim 1, wherein: the first member is a disc-shaped channel.

3. A cyclonic micro reaction channel as claimed in claim 1, wherein: the second part is a connecting channel which is an arc-shaped channel, and the arc-shaped channel is bent towards the first part;

or the second part is a connecting channel which comprises a section of linear channel and a section of arc channel which are connected, and the arc channel bends to the first part.

4. A cyclonic micro reaction channel as claimed in claim 1, wherein: the joint of the second reaction unit and the first reaction unit is arranged at the central position of the first part of the first reaction unit.

5. A cyclonic micro reaction channel as claimed in claim 1, wherein: the input section is a first reaction unit/a third reaction unit and is provided with at least two inlets;

or the output section is a first reaction unit/a third reaction unit and is provided with at least one outlet.

6. A micro-reaction substrate is characterized in that: the substrate comprises a substrate body, wherein a plurality of rows of first reaction units are arranged on the substrate body, the first reaction units positioned in the same row are arranged at intervals and in the same direction, and the first reaction units in adjacent rows are arranged oppositely;

or, an input section or/and an output section are also arranged;

or, comprising a substrate body on which the swirling micro reaction channel of any one of claims 1 to 5 is provided.

7. A micro-reactor is characterized in that: the device comprises a first reaction substrate, a second reaction substrate and a third reaction substrate which are arranged in parallel, wherein an input section or/and an output section and a plurality of rows of first reaction units in the same plane are arranged on the contact surface of the first reaction substrate and the second reaction substrate, the first reaction units in the same row are arranged at intervals and in the same direction, the first reaction units in adjacent rows are arranged oppositely, and each first reaction unit comprises a first part for keeping fluid to flow in a rotating manner and a second part tangentially connected with the first part;

a plurality of rows of penetrating second reaction units are arranged on the second reaction substrate;

a plurality of rows of third reaction units in the same plane are arranged on the contact surface of the third reaction substrate and the second reaction substrate, the third reaction units have the same structure as the first reaction units, are staggered with the first reaction units in the vertical direction and are oppositely arranged in the horizontal direction;

or, comprising at least one reaction substrate, on the substrate body of which a swirling micro reaction channel according to any of claims 1-5 is provided.

8. A microreactor as claimed in claim 7 wherein: the device also comprises a first end plate and a second end plate, wherein the first end plate and the second end plate are respectively arranged at the outer side of the microreactor;

the plates are detachably connected or integrally and non-detachably connected.

9. A microreactor as claimed in claim 8, wherein: and a sealing structure is arranged between the plates.

10. A micro-reaction system, characterized by: comprising a plurality of microreactors according to any of claims 7-9 in series or in parallel.

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