CN108014730A - A kind of microreactor and chemical producing system - Google Patents
A kind of microreactor and chemical producing system Download PDFInfo
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- CN108014730A CN108014730A CN201711465461.6A CN201711465461A CN108014730A CN 108014730 A CN108014730 A CN 108014730A CN 201711465461 A CN201711465461 A CN 201711465461A CN 108014730 A CN108014730 A CN 108014730A
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- 239000000126 substance Substances 0.000 title claims abstract description 13
- 238000006243 chemical reaction Methods 0.000 claims abstract description 123
- 239000000411 inducer Substances 0.000 claims description 17
- 230000000694 effects Effects 0.000 abstract description 24
- 239000012530 fluid Substances 0.000 abstract description 9
- 238000004519 manufacturing process Methods 0.000 abstract description 7
- 239000000463 material Substances 0.000 description 13
- 238000010586 diagram Methods 0.000 description 4
- 230000035939 shock Effects 0.000 description 4
- 238000007599 discharging Methods 0.000 description 3
- 238000009434 installation Methods 0.000 description 3
- 239000000376 reactant Substances 0.000 description 3
- 238000003491 array Methods 0.000 description 2
- 238000005452 bending Methods 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 238000009792 diffusion process Methods 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 238000000034 method Methods 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000006722 reduction reaction Methods 0.000 description 1
- 230000004044 response Effects 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000003466 welding Methods 0.000 description 1
Classifications
-
- 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
-
- 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
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00781—Aspects relating to microreactors
- B01J2219/00788—Three-dimensional assemblies, i.e. the reactor comprising a form other than a stack of plates
- B01J2219/00792—One or more tube-shaped elements
- B01J2219/00795—Spiral-shaped
-
- 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
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00781—Aspects relating to microreactors
- B01J2219/00891—Feeding or evacuation
- B01J2219/00894—More than two inlets
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
Abstract
The present invention provides a kind of microreactor and chemical producing system, is related to chemical reaction equipment field.It includes：Cylinder, cylinder limit accommodating cavity.Cylinder is provided with feed pipe, and feed pipe is interconnected with accommodating cavity.Further include reaction tube, reaction tube helically type and is arranged in accommodating cavity, and the both ends of reaction tube through cylinder and are extended to outside cylinder.Coiled coil adds coiling length of the reaction tube in same space, increases the heat exchange area of heat transferring medium and reaction mass under the conditions of enabling reaction tube in a limited space, improves heat exchange efficiency.Coiled coil also further increases mass transfer effect of the fluid in reaction tube at the same time.Mass transfer effect and heat-transfer effect are improved at the same time, make the reaction uniformity higher of reaction mass, reaction yield higher.The present invention also provides a kind of chemical producing system, including above-mentioned microreactor.The chemical producing system utilizes the high efficient heat exchanging ability of microreactor, can achieve the purpose that to improve production efficiency and production capacity.
Description
Technical field
The present invention relates to chemical reaction equipment field, in particular to a kind of microreactor and chemical producing system.
Background technology
Reaction unit is one of common device of chemical field.Violent heat release is frequently accompanied by chemical reaction,
And heat cannot exclude in time, the rising of reaction process temperature can be caused, influence being normally carried out for reaction, reduce reaction yield.
In order to improve the mixing of reactant and heat transfer efficiency, there is a kind of microreactor.Although current existing microreactor is compared
Increase in the heat-transfer effect of traditional reactor, but requirement of the industry for chemical reaction is also higher and higher, therefore micro- reaction
The heat-transfer effect of device still has much room for improvement.
The content of the invention
It is an object of the invention to provide a kind of microreactor, it has higher exchange capability of heat, can make reaction process
In heat transfer and temperature be controlled better.
Another object of the present invention is to provide a kind of chemical producing system, it can utilize the higher heat exchange of microreactor
Ability achievees the purpose that to improve production efficiency.
What the embodiment of the present invention was realized in：
A kind of microreactor, including：
Cylinder, cylinder limit accommodating cavity.Cylinder is provided with feed pipe, and feed pipe is interconnected with accommodating cavity.
Reaction tube, reaction tube helically type and are arranged in accommodating cavity, and the both ends of reaction tube through cylinder and extend
To outside cylinder.
Further, cylinder is provided with multiple feed pipes, and at least two feed pipes have different angles of inclination.
Further, the discharge nozzle for being installed on cylinder is further included.Feed pipe, accommodating cavity and discharge nozzle are sequentially communicated.Into
Expects pipe is relatively arranged on the both ends of cylinder with discharge nozzle, and reaction tube is between feed pipe and discharge nozzle.
Further, a diameter of 3-8 millimeters of reaction tube.
Further, the outlet face of the section tubular wall of reaction tube and at least one feed pipe.
Further, reaction tube includes interconnected the first helix tube and the second helix tube.First helix tube and second
Helix tube is respectively positioned in accommodating cavity, and the second helix tube is surround by the first helix tube.
Further, the first helix tube is used to reaction mass being directed into accommodating cavity, and the second helix tube is used for will be anti-
Material is answered to export to outside accommodating cavity.
Further, the outlet section of the inducer of the first helix tube and the second helix tube through cylinder and extends to cylinder
Outside.
Further, inducer and outlet section are located at the same plane of cylinder radially.
Further, flow-disturbing component is set in reaction tube, and flow-disturbing component is detachably connected with reaction tube.
Further, flow-disturbing component includes the different first baffles and second baffle in angle of inclination.
Further, first baffle and/or second baffle open up multiple through holes.
A kind of chemical producing system, including any one above-mentioned microreactor.
The embodiment of the present invention at least has the following advantages that or beneficial effect：
The embodiment of the present invention provides a kind of microreactor, it mainly includes cylinder and reaction tube.Wherein, cylinder be provided with into
Expects pipe, and the accommodating cavity that feed pipe is limited with cylinder is interconnected, and to be fed by feed pipe, ensures that charging is filled
Foot.Reaction tube helically type and is arranged in accommodating cavity, and the both ends of reaction tube through cylinder and are extended to outside cylinder, are easy to
The charging and discharging of reaction tube.Coiled coil adds coiling length of the reaction tube in same space, reaction tube is existed
Increase the heat exchange area of heat transferring medium and reaction mass under limited steric requirements, improve heat exchange efficiency.Coiled coil at the same time
Further increase mass transfer effect of the fluid in reaction tube.Mass transfer effect and heat-transfer effect are improved at the same time, make reactant
The reaction uniformity higher of material, reaction yield higher.
The embodiment of the present invention also provides a kind of chemical producing system, including above-mentioned microreactor.Chemical producing system profit
With the high efficient heat exchanging ability of microreactor, can achieve the purpose that to improve production efficiency and production capacity.
Brief description of the drawings
In order to illustrate the technical solution of the embodiments of the present invention more clearly, below will be to needed in the embodiment attached
Figure is briefly described, it will be appreciated that the following drawings illustrate only certain embodiments of the present invention, therefore be not construed as pair
The restriction of scope, for those of ordinary skill in the art, without creative efforts, can also be according to this
A little attached drawings obtain other relevant attached drawings.
Fig. 1 is the structure diagram of microreactor 100 provided in an embodiment of the present invention；
Fig. 2 is the A direction views of Fig. 1；
Fig. 3 is the B direction views of Fig. 1；
Fig. 4 is the structure diagram of flow-disturbing component provided in an embodiment of the present invention.
Icon：100- microreactors；110- cylinders；112- accommodating cavities；114- feed pipes；116- discharge nozzles；150- is anti-
Ying Guan；The first helix tubes of 152-；The second helix tubes of 154-；156- bending sections；158- inducers；160- outlet sections；162- flow-disturbings
Component；164- fixed cylinders；166- first baffles；168- second baffles；170- through holes.
Embodiment
To make the purpose, technical scheme and advantage of the embodiment of the present invention clearer, below in conjunction with the embodiment of the present invention
In attached drawing, the technical solution in the embodiment of the present invention is clearly and completely described, it is clear that described embodiment is
Part of the embodiment of the present invention, instead of all the embodiments.The present invention implementation being usually described and illustrated herein in the accompanying drawings
The component of example can be arranged and designed with a variety of configurations.
Therefore, below the detailed description of the embodiment of the present invention to providing in the accompanying drawings be not intended to limit it is claimed
The scope of the present invention, but be merely representative of the present invention selected embodiment.Based on the embodiments of the present invention, this area is common
Technical staff's all other embodiments obtained without creative efforts, belong to the model that the present invention protects
Enclose.
It should be noted that：Similar label and letter represents similar terms in following attached drawing, therefore, once a certain Xiang Yi
It is defined, then it further need not be defined and explained in subsequent attached drawing in a attached drawing.
, it is necessary to explanation in the description of the embodiment of the present invention, if there is the finger such as term " on ", " under ", " interior ", " outer "
The orientation or position relationship shown is based on orientation shown in the drawings or position relationship, or is usually put during the invention product use
The orientation or position relationship put, are for only for ease of the description present invention and simplify description, rather than instruction or the dress for implying meaning
Put or element there must be specific orientation, with specific azimuth configuration and operation, therefore it is not intended that to limit of the invention
System.In addition, term " first ", " second " etc. are only used for distinguishing description, and it is not intended that instruction or hint relative importance.
In the description of the embodiment of the present invention, it is also necessary to explanation, unless otherwise clearly defined and limited, if occurring
Term " setting ", " installation ", " connection " should be interpreted broadly, for example, it may be fixedly connected or be detachably connected,
Or it is integrally connected；It can be directly connected, can also be indirectly connected by intermediary, can be the company inside two elements
It is logical.For the ordinary skill in the art, the concrete meaning of above-mentioned term in the present invention can be understood with concrete condition.
Embodiment
Fig. 1 is refer to, Fig. 1 show the structure diagram of microreactor 100.The present embodiment provides a kind of microreactor
100, it is mainly used for providing reacting environment and suitable reaction condition for chemical reaction.
Microreactor 100 includes the cylinder 110 and reaction tube 150 being connected with each other.Reaction tube 150 is installed in cylinder 110,
And the both ends of reaction tube 150 through cylinder 110 and are extended to outside cylinder 110, easy to the charging and discharging of reaction tube 150.Its
In, the diameter of reaction tube 150 is generally 3-8 millimeters.
It is used to contain heat transferring medium in the present embodiment, in cylinder 110, reaction tube 150 is used to contain reaction mass.It is available
Heat transferring medium is heated up or is cooled down to reaction mass, so that reaction mass is under suitable reaction temperature.
Cylinder 110 limits accommodating cavity 112, and reaction tube 150 is located in accommodating cavity 112.Accommodating cavity 112 is used to contain
Heat transferring medium.
Multiple (at least two) feed pipes 114 are installed on cylinder 110, each feed pipe 114 with 112 phase of accommodating cavity
It is intercommunicated.Feed pipe 114 is used to import heat transferring medium into accommodating cavity 112.In this implementation, 9 feed pipes 114 are employed,
And 9 feed pipes 114 are mounted on the end face of 110 one end of cylinder.The setting can extend connecing for heat transferring medium and reaction tube 150
The time is touched, heat transferring medium is come into full contact with reaction tube 150.Heat transferring medium comes into full contact with reaction tube 150 can be significantly
Strengthen the heat transfer effect of heat transferring medium and reaction mass.Certainly, in other embodiment, the quantity and installation site of feed pipe 114
It can be adjusted accordingly, such as feed pipe 114 can be installed on the side face of cylinder 110 according to specific requirements.
In all feed pipes 114, at least two feed pipes 114 have different angles of inclination, i.e. at least two feed pipes
114 outlet has different directions so that and the shock possibility with higher when material flows out, produces vortex in material,
So as to strengthen the heat transfer effect of material.Shock form includes mutually the hitting between shock, material and cylinder 110 between material
Hit, shock between material and reaction tube 150 etc..As shown in Figure 1,9 feed pipes 114 have 5 kinds of inclinations angle in the present embodiment
Degree.Reaction tube 150,114 caliber of feed pipe are smaller, and inventor, which studies, to be found, under this kind of state, heat transferring medium and reaction mass
Flowing laminar condition is easily presented.Laminar flow and turbulent flow belong to the flow regime of fluid.Fluid is in Bottomhole pressure, its particle
Make smooth linear motion along the direction parallel with pipe axis, such a flowing is known as laminar flow or viscous flow, also there is referred to as streamlined flow.
When turbulent, the streamline of fluid is no longer clearly apparent, the small whirlpool in many of flow field, and fluid flowing has obvious randomness and expansion
Property is dissipated, and this diffusion includes mass transfer, heat transfer and the diffusion for transmitting the forms such as momentum.Under laminar condition, heat transferring medium and reaction
The heat transfer effect of material will be greatly reduced.The feed pipe 114 installed in the present embodiment has different angles of inclination so that heat exchange
It can be entered after medium outflow feed pipe 114 with different ejection angles in accommodating cavity 112, so as to improve heat transferring medium
Between mutual collision probability, the collision probability of heat transferring medium and reaction tube 150, the collision probability of heat transferring medium and cylinder 110,
Collision makes laminar flow be changed into turbulent flow, and then improves the heat exchange efficiency of heat transferring medium, strengthens the heat transfer effect of microreactor 100.
Discharge nozzle 116 is also equipped with cylinder 110, easy to the discharging of heat transferring medium.Feed pipe 114,112 and of accommodating cavity
Discharge nozzle 116 is sequentially communicated.In the present embodiment, discharge nozzle 116 and feed pipe 114 are relatively arranged on the both ends of cylinder 110, that is, go out
Expects pipe 116 is installed on the end face of 110 other end of cylinder.Reaction tube 150 is between feed pipe 114 and discharge nozzle 116.This kind
Under setting, the time that heat transferring medium has abundance contacts with reaction tube 150, improves the utilization rate of heat transferring medium, enhances heat exchange
Effect.
In the present embodiment, cylinder 110 is in cylindrical type, and it is also cylindrical type that reaction tube 150, which limits the shape formed,.Both shapes
When shape is identical, the uniform throughout of the heat transferring medium that is more advantageous in cylinder 110 and reaction tube 150, come into full contact with, to improve heat exchange
Efficiency.Certainly, in other embodiment, the shape that 150 outermost of reaction tube limits can also be other shapes, such as cone,
Spherical, square etc., cylinder 110 can select same shape, can also select different shapes.
In the present embodiment, the helically type of reaction tube 150, as shown in Figure 1, reaction tube 150 is spiral extremely by one end of cylinder 110
The other end of cylinder 110, the shape of spiralization is cylindrical type.The setting of screw type can in a limited space under the conditions of increase
Add the heat exchange area of heat transferring medium and reaction mass, improve heat exchange efficiency.Certainly, in other embodiment, reaction tube 150 can also
It is configured with other arrangement modes, such as U-shaped, multiple straight tube arrays, multiple helix tube arrays etc..
To ensure the collision of reaction tube 150 and heat transferring medium, the section tubular wall and at least one of reaction tube 150 in the present embodiment
The outlet face of a feed pipe 114.When in the feed pipe 114 heat transferring medium outflow when, this part heat transferring medium will directly with
The tube wall of reaction tube 150 produces collision, so that the collision and heat transferring medium between triggering heat transferring medium and the collision of cylinder 110,
And then change the laminar condition of heat transferring medium, improve the heat exchange efficiency of heat transferring medium.
In the present embodiment, reaction tube 150 includes interconnected the first helix tube 152 and the second helix tube 154.First spiral shell
152 and second helix tube 154 of coil passes through 156 rounding off of bending section.154 equal position of first helix tube 152 and the second helix tube
In in accommodating cavity 112, the second helix tube 154 is surround by the first helix tube 152.The arrangement mode of inside and outside two layers of spiral pipes can
Further increase heat exchange area, while also make it that heat exchange area distribution is more uniform, make the temperature in reaction tube 150 everywhere consistent
Property higher, be conducive to more accurately and comprehensively control the temperature of reaction mass, reduce the generation of side reaction, improve reaction yield, together
The Shi Jieyue occupied spaces of microreactor 100.Certainly, in other embodiment, the number of plies of helix tube can also further be increased
Or a helical layer pipe is only set.In addition, the deformation of multi-layer helix-tube in order to prevent, branch can be further set in other embodiment
Support member is used to support reaction tube 150.
Further, the outlet section 160 of 158 and second helix tube 154 of inducer of the first helix tube 152 runs through cylinder
110 and extend to outside cylinder 110.Reaction mass is fed by inducer 158, in the first helix tube 152 and the second helix tube 154
After reacting, discharged by outlet section 160.As shown in Figure 1, reaction mass, along after 152 spiral of the first helix tube, process is curved
Tune 156 transits to the second helix tube 154 and drops to outlet section 160 along the second helix tube 154 is spiral.It refer to Fig. 2 and figure
3, Fig. 2 show the A direction views of Fig. 1, and Fig. 3 show the B direction views of Fig. 1.According to Fig. 1, Fig. 2 and Fig. 3, the present embodiment
In, inducer 158 and outlet section 160 are located at the same plane of cylinder 110 radially.The setting can make full use of the spiral shell of multilayer
Space is revolved, reaction mass is sufficiently reacted, also further improves the temperature uniformity of reaction mass everywhere, be conducive to carry
High reaction yield.Certainly, in other embodiment, the relative position of inducer 158 and outlet section 160 can according to specific requirements into
The corresponding adjustment of row.It can also feed from outlet section 160 in other embodiment, be discharged by inducer 158.
Fig. 4 is refer to, Fig. 4 show the structure diagram of flow-disturbing component 162.In the present embodiment, may be used also in reaction tube 150
Further to set flow-disturbing component 162, when reaction mass flows through flow-disturbing component 162,162 one side of flow-disturbing component makes reactant
Mixed effect enhancing between material, on the other hand destroys the laminar condition of reaction mass, strengthen reaction mass and heat transferring medium it
Between heat transfer effect and reaction mass between mass transfer effect.In the present embodiment, flow-disturbing component 162 and reaction tube 150 are detachable
Connection, when the reaction between reaction mass is strong exothermal reaction, flow-disturbing component 162 can be removed, avoid heat cannot and
When export.The mode being detachably connected can be a variety of, such as be threadedly coupled, clamping etc..
Flow-disturbing component 162 can be arranged on the optional position of reaction tube 150.In the present embodiment, flow-disturbing component 162 is arranged on
In inducer 158, entered easy to reaction mass with preferable flow regime in the first helix tube 152.Certainly, other embodiment
In, can also be in the multiple flow-disturbing components 162 of each position spaced set of reaction tube 150.
Flow-disturbing component 162 includes fixed cylinder 164, first baffle 166 and second baffle 168.First baffle 166 and second gear
Plate 168 has different angles of inclination, and is mounted in fixed cylinder 164., can also be straight by two baffles in other embodiment
Connect to be installed in inducer 158 and carry out flow-disturbing.The baffle of differing tilt angles can carry out flow-disturbing to reaction mass, so as to change
The flow regime of reaction mass, strengthens heat transfer effect and mass transfer effect.Certainly, in other embodiment, can be disturbed using others
Flow structure, such as filled solid filler or the quantity and installation site of changing baffle.The diameter of fixed cylinder 164 can be with inducer
158 diameter is identical, is connected easy to inducer 158 with the matching of fixed cylinder 164.Certainly, in other embodiment, fixed cylinder 164
It can also be other shapes, fixed cylinder 164 can also be connected on inducer 158 by welding.
Further, in the present embodiment, multiple through holes 170 is opened up on first baffle 166 and second baffle 168, are used for
Reduction reaction mass flows through the pressure drop before and after flow-disturbing component 162.Fluid fluid overcomes internal friction and overcomes turbulent flow when flowing when
The front and rear place that momentum causes fluid to flow mutually is collided and exchanged between particle and produces pressure differential, is pressure drop.Pressure drop is excessive not only
It is unfavorable for the security of microreactor 100, also the reaction effect for making reaction mass is deteriorated.
The operation principle of microreactor 100 is：
Heat transferring medium is entered in accommodating cavity 112 by feed pipe 114, can be after heat transferring medium is full of accommodating cavity 112
The feeding work of reaction mass is carried out again, to improve the heat exchange uniformity of reaction mass everywhere.Continuous production process, generally needs
Discharge nozzle 116 is opened, allows that heat transferring medium is continuous, circulation carries out heat exchange.Heat transferring medium by multiple feed pipes 114 into
When entering accommodating cavity 112, there is multiple and different spray angles, the jet flow of different directions and collision, make tool inside heat transferring medium
There is different flow directions, managed so as to be internally formed multiple vortexs in heat transferring medium and then strengthen heat transferring medium with reaction tube 150
The heat convection of wall, achievees the purpose that to strengthen heat transferring medium and reaction mass heat transfer effect.Reaction mass by inducer 158 successively
The first helix tube 152, the second helix tube 154 are flowed through, reaction, the heat exchange of reaction mass are also concentrated mainly on the first helix tube 152
Carried out with the second helix tube 154, two layers of spiral pipes makes reaction mass adequately and uniformly be reacted and exchanged heat, final reaction
Material is flowed out by outlet section 160.Reaction mass will be subject to the flow-disturbing of flow-disturbing component 162 after entering inducer 158, so as to improve anti-
Answer the mass transfer effect of material, while the heat transfer effect of intensified response material and heat transferring medium.The mass transfer effect of microreactor 100 and
Heat-transfer effect is strengthened at the same time, greatly promotes the heat transfer in reaction process and temperature-controllable higher, reaction yield.
The present embodiment also provides a kind of chemical producing system, including microreactor 100, its have higher production capacity and
Production efficiency.
It these are only the preferred embodiment of the present invention, be not intended to limit the invention, for those skilled in the art
For member, the invention may be variously modified and varied.Any modification within the spirit and principles of the invention, being made,
Equivalent substitution, improvement etc., should all be included in the protection scope of the present invention.
Claims (13)
- A kind of 1. microreactor, it is characterised in that including：Cylinder, the cylinder limit accommodating cavity, and the cylinder is provided with feed pipe, the feed pipe and the accommodating cavity phase It is intercommunicated；Reaction tube, the reaction tube helically type and are arranged in the accommodating cavity, and institute is run through at the both ends of the reaction tube State cylinder and extend to outside the cylinder.
- 2. microreactor according to claim 1, it is characterised in that：The cylinder is provided with multiple feed pipes, and at least two feed pipes have different angles of inclination.
- 3. microreactor according to claim 1, it is characterised in that：The discharge nozzle for being installed on the cylinder is further included, the feed pipe, the accommodating cavity and the discharge nozzle are sequentially communicated, The feed pipe and the discharge nozzle are relatively arranged on the both ends of the cylinder, the reaction tube be located at the feed pipe with it is described Between discharge nozzle.
- 4. microreactor according to claim 1, it is characterised in that：A diameter of 3-8 millimeters of the reaction tube.
- 5. microreactor according to claim 1, it is characterised in that：The outlet face of the section tubular wall of the reaction tube and at least one feed pipe.
- 6. according to claim 1 any one of them microreactor, it is characterised in that：The reaction tube includes interconnected the first helix tube and the second helix tube, first helix tube and second spiral shell Coil is respectively positioned in the accommodating cavity, and second helix tube is surround by first helix tube.
- 7. microreactor according to claim 6, it is characterised in that：First helix tube is used to reaction mass being directed into the accommodating cavity, and second helix tube is used for by described in Reaction mass is exported to outside the accommodating cavity.
- 8. microreactor according to claim 6, it is characterised in that：The inducer of first helix tube and the outlet section of second helix tube through the cylinder and extend to described Outside cylinder.
- 9. microreactor according to claim 8, it is characterised in that：The inducer and the outlet section are located at the same plane of the cylinder radially.
- 10. according to claim 1-9 any one of them microreactors, it is characterised in that：Flow-disturbing component is set in the reaction tube, and the flow-disturbing component is detachably connected with the reaction tube.
- 11. microreactor according to claim 10, it is characterised in that：The flow-disturbing component includes the different first baffles and second baffle in angle of inclination.
- 12. microreactor according to claim 11, it is characterised in that：The first baffle and/or the second baffle open up multiple through holes.
- A kind of 13. chemical producing system, it is characterised in that：Including such as claim 1-12 any one of them microreactor.
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| CN201711465461.6A CN108014730B (en) | 2017-12-28 | 2017-12-28 | Microreactor and chemical production system |
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| CN201711465461.6A CN108014730B (en) | 2017-12-28 | 2017-12-28 | Microreactor and chemical production system |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108745261A (en) * | 2018-06-04 | 2018-11-06 | 西安交通大学 | A kind of multiple-unit metal hydride accumulation of heat reactor |
| CN109894069A (en) * | 2019-04-23 | 2019-06-18 | 大连鼎燕医药化工有限公司 | It is used to prepare the thermal decomposition reactor and its system, continuous preparation process of fluorinated aromatic hydrocarbon |
| CN109925991A (en) * | 2019-04-19 | 2019-06-25 | 山东豪迈化工技术有限公司 | Micro passage reaction |
| CN114870766A (en) * | 2022-05-31 | 2022-08-09 | 浙江大学 | Series-wound coil type micro-reactor system for nitration reaction |
Citations (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0123653A1 (en) * | 1983-04-22 | 1984-10-31 | Kurier Holding AG | Static heat exchanger with high efficiency in particular suitable for the cooling of viscous fluids |
| SU1125040A1 (en) * | 1982-05-14 | 1984-11-23 | Предприятие П/Я Р-6956 | Gas-liquid reactor |
| JPH10339587A (en) * | 1997-06-10 | 1998-12-22 | Nippon Light Metal Co Ltd | Heat exchanger |
| JPH10339592A (en) * | 1997-06-05 | 1998-12-22 | Akutoronikusu Kk | Pressure proof structured thin plate heat pipe and manufacture thereof |
| CN2581931Y (en) * | 2002-07-05 | 2003-10-22 | 宋小平 | Heat exchanger |
| CN101450300A (en) * | 2007-12-05 | 2009-06-10 | 海南大学 | Continuous current micro-reactor and preparation method and use thereof |
| CN101968330A (en) * | 2010-10-28 | 2011-02-09 | 湖北登峰换热器有限公司 | Built-in strengthening flap type heat exchange tube |
| CN202734623U (en) * | 2012-06-28 | 2013-02-13 | 苏州市富帮金属制品有限公司 | Baffled heat exchanger |
| JP2013257051A (en) * | 2012-06-11 | 2013-12-26 | Fujifilm Corp | Horizontal heat exchanger, and condensation apparatus |
| CN103801245A (en) * | 2014-01-27 | 2014-05-21 | 石祖嘉 | Tubular type double-annular channel double-sided heat-exchange large-flux microchannel reactor |
| CN104258796A (en) * | 2014-10-13 | 2015-01-07 | 南京工业大学 | Novel high-flux multilayer spiral winding pipe micro-channel reactor |
| CN107999012A (en) * | 2017-12-28 | 2018-05-08 | 山东豪迈化工技术有限公司 | A kind of reactor and chemical producing system |
| CN207941501U (en) * | 2017-12-28 | 2018-10-09 | 山东豪迈化工技术有限公司 | A kind of microreactor and chemical producing system |
-
2017
- 2017-12-28 CN CN201711465461.6A patent/CN108014730B/en active Active
Patent Citations (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| SU1125040A1 (en) * | 1982-05-14 | 1984-11-23 | Предприятие П/Я Р-6956 | Gas-liquid reactor |
| EP0123653A1 (en) * | 1983-04-22 | 1984-10-31 | Kurier Holding AG | Static heat exchanger with high efficiency in particular suitable for the cooling of viscous fluids |
| JPH10339592A (en) * | 1997-06-05 | 1998-12-22 | Akutoronikusu Kk | Pressure proof structured thin plate heat pipe and manufacture thereof |
| JPH10339587A (en) * | 1997-06-10 | 1998-12-22 | Nippon Light Metal Co Ltd | Heat exchanger |
| CN2581931Y (en) * | 2002-07-05 | 2003-10-22 | 宋小平 | Heat exchanger |
| CN101450300A (en) * | 2007-12-05 | 2009-06-10 | 海南大学 | Continuous current micro-reactor and preparation method and use thereof |
| CN101968330A (en) * | 2010-10-28 | 2011-02-09 | 湖北登峰换热器有限公司 | Built-in strengthening flap type heat exchange tube |
| JP2013257051A (en) * | 2012-06-11 | 2013-12-26 | Fujifilm Corp | Horizontal heat exchanger, and condensation apparatus |
| CN202734623U (en) * | 2012-06-28 | 2013-02-13 | 苏州市富帮金属制品有限公司 | Baffled heat exchanger |
| CN103801245A (en) * | 2014-01-27 | 2014-05-21 | 石祖嘉 | Tubular type double-annular channel double-sided heat-exchange large-flux microchannel reactor |
| CN104258796A (en) * | 2014-10-13 | 2015-01-07 | 南京工业大学 | Novel high-flux multilayer spiral winding pipe micro-channel reactor |
| CN107999012A (en) * | 2017-12-28 | 2018-05-08 | 山东豪迈化工技术有限公司 | A kind of reactor and chemical producing system |
| CN207941501U (en) * | 2017-12-28 | 2018-10-09 | 山东豪迈化工技术有限公司 | A kind of microreactor and chemical producing system |
Non-Patent Citations (2)
| Title |
|---|
| 李凡等人: "空气源热泵热水器", 重庆大学出版社, pages: 63 * |
| 金浩哲;陈小平;郑智剑;偶国富;舒歌平;王超;贺亮;: "挡板倾斜角度对热高压分离器内颗粒漂移影响的数值模拟", 煤炭学报, no. 08, 15 August 2016 (2016-08-15), pages 63 * |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108745261A (en) * | 2018-06-04 | 2018-11-06 | 西安交通大学 | A kind of multiple-unit metal hydride accumulation of heat reactor |
| CN109925991A (en) * | 2019-04-19 | 2019-06-25 | 山东豪迈化工技术有限公司 | Micro passage reaction |
| CN109925991B (en) * | 2019-04-19 | 2024-04-19 | 山东豪迈化工技术有限公司 | Microchannel reactor |
| CN109894069A (en) * | 2019-04-23 | 2019-06-18 | 大连鼎燕医药化工有限公司 | It is used to prepare the thermal decomposition reactor and its system, continuous preparation process of fluorinated aromatic hydrocarbon |
| CN114870766A (en) * | 2022-05-31 | 2022-08-09 | 浙江大学 | Series-wound coil type micro-reactor system for nitration reaction |
| CN114870766B (en) * | 2022-05-31 | 2023-01-10 | 浙江大学 | Series-wound coil type microreactor system for nitration reaction |
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