CN208975763U - A kind of multichannel microreactor - Google Patents
A kind of multichannel microreactor Download PDFInfo
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- CN208975763U CN208975763U CN201821064649.XU CN201821064649U CN208975763U CN 208975763 U CN208975763 U CN 208975763U CN 201821064649 U CN201821064649 U CN 201821064649U CN 208975763 U CN208975763 U CN 208975763U
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Abstract
A kind of multichannel microreactor, successively include distributing chamber (6), reacting replacing heat area and collecting chamber (5), distributed component (13) are set in the distributing chamber (6), the reacting replacing heat area is made of multiple reaction channels (9) and adjacent heat exchanger channels (8), hybrid component (10) are set in the reaction channel, the microreactor entrance (2) is through distributing chamber (6), reaction channel (9), collecting chamber (5) and microreactor outlet (1) are sequentially communicated, the heat transferring medium entrance (4) is connected to through heat exchanger channels with heat transferring medium outlet (3).Multichannel microreactor provided by the utility model can keep reacting replacing heat process to stablize, and can strengthen the progress of reaction process, improve conversion ratio and shorten the reaction time.
Description
Technical field
The utility model relates to a kind of multichannel microreactors, and it is poly- to be suitable for continuous synthesis more specifically to one kind
The reactor of alpha olefine synthetic oil.
Background technique
Poly alpha olefine synthetic oil (PAO) is a kind of top-grade lubricating oil base oil, is had in fields such as military project, aerospaces
Important purposes.PAO has the characteristics that Viscosity Index is high, volatility is low, mobility is low and cutting performance is good, and in high temperature item
There is good oxygen stability under part.
CN101054332A discloses a kind of method that two kettles interval in parallel synthesizes PAO.With BF3For catalyst, it is with alcohol
Initiator reacts 1~6h, available PAO under 0~80 DEG C, the reaction condition of 0~1MPa, the tetramer (PAO- in product
4) at most.
US4045508 discloses the method for continuous two-stage synthesis PAO a kind of.The first order uses continuous stirred tank, built-in to take
Hot coil, the second level are the tubular reactor being immersed in heat transferring medium.By changing experiment condition, may be implemented three in product
The change of aggressiveness (PAO-3) and tetramer ratio.
In general, PAO synthesis device mostly uses the form of stirred tank at present.With the increase for the treatment of capacity, stirred tank
Amplification can be more and more difficult, and will lead to material and generate apparent residence time destribution, and then influence tripolymer and the tetramer etc.
The selectivity of important products.Therefore in order to eliminate the influence of residence time destribution, it is necessary to which it is flat to approach that exploitation is able to maintain that material
The flow reactor that the form of plug-flow is flowed, to guarantee PAO large-scale industrial production.
Utility model content
The technical problem to be solved by the present invention is to provide a kind of multichannel microreactor, which is applicable in
In the reactor as continuous synthesizing poly alpha-olefin synthetic oil.
The multichannel microreactor that the utility model supplies, it is described successively including distributing chamber 6, reacting replacing heat area and collecting chamber 5
Distributing chamber 6 in distributed component 13 is set, the reacting replacing heat area is by multiple reaction channels 9 and adjacent 8 groups of heat exchanger channels
At setting hybrid component 10 in the reaction channel, the interior setting heat exchange partition 12 of the heat exchanger channels 8, described is micro- anti-
Device entrance 2 is answered to be sequentially communicated through distributing chamber 6, reaction channel 9, collecting chamber 5 and microreactor outlet 1, heat transferring medium entrance 4 is through changing
The passage of heat is connected to heat transferring medium outlet 3.
The operation condition of multichannel microreactor provided by the utility model are as follows: reaction pressure is 0.1~4MPa,
Reaction temperature is 0~100 DEG C.
Multichannel microreactor provided by the utility model has the beneficial effect that
Multichannel microreactor provided by the utility model is suitable for the synthesis reactor of poly alpha olefine synthetic oil (PAO),
Compared with the reactor of the synthesis of PAO disclosed in the prior art, multichannel microreactor provided by the utility model is able to maintain
The flowing of fluid approximation plug flow can guarantee the consistency of reacting fluid residence time as far as possible, avoid due to the residence time
Undesirable selectivity of product caused by distribution.Since heat exchanger channels volume is much larger than reaction channel volume, it is ensured that reaction
Heat transfer process is stablized, and the ideal reaction time is maintained.Hybrid component is equipped in reaction channel, can strengthen reaction process into
Row improves conversion ratio, shortens the reaction time.Setting heat exchange partition can be further improved heat exchange efficiency.
Detailed description of the invention
Fig. 1 is multichannel microreactor structural schematic diagram provided by the utility model.
Wherein: the outlet of 1- microreactor；2- microreactor entrance；The outlet of 3- heat transferring medium；4- heat transferring medium entrance；5- is received
Collect room；6- distributing chamber；7- reactor shell；8- heat exchanger channels；9- reaction channel；10- hybrid component；11- tube sheet；12- heat exchange
Partition；13- distributed component.
Specific embodiment
Multichannel microreactor provided by the utility model is embodied in this way:
Multichannel microreactor provided by the utility model successively includes distributing chamber 6, reacting replacing heat area and collecting chamber 5, institute
Distributed component 13 is set in the distributing chamber 6 stated, and the reacting replacing heat area is by multiple reaction channels 9 and adjacent heat exchanger channels 8
Composition, is arranged hybrid component 10 in the reaction channel, the microreactor entrance 2 through distributing chamber 6, reaction channel 9,
Collecting chamber 5 and microreactor outlet 1 are sequentially communicated, and heat transferring medium entrance 4 is connected to through heat exchanger channels with heat transferring medium outlet 3.
In multichannel microreactor provided by the utility model, the cross-sectional area of the reaction channel 9 is 1~
150mm2, preferably 10~120mm2, length is between the two neighboring reaction channel of 50~5000mm, preferably 100~3000mm
Distance be 1~50mm, preferably 3~30mm.
The shape of the cross section of the reaction channel 9 can be rectangle, circle or other shapes, preferably rectangle.
Since flow area is small, flow velocity of the fluid in reaction channel is high, and can keep flow process is plug flow, reduces the residence time
The influence of distribution.
The hybrid component being arranged in the reaction channel, hybrid component can for cross-fin, corrugated board structures or its
His porous media, preferably cross-fin structure or corrugated board structures.The hybrid component can be strengthened in reaction channel
The reaction time is shortened in the mixing and reaction process of fluid.
In multichannel microreactor provided by the utility model, distributed component is set in the distributing chamber, it is preferably described
Distributed component there is distribution hole or item to stitch, the distributed component has and can be uniformly distributed the knot for being distributed indoor fluid
Structure guarantees that the fluid flow in each reaction channel is almost the same.
In multichannel microreactor provided by the utility model, the volumetric ratio of the heat exchanger channels and reaction channel is 4
~30:1, preferably 5~20:1.The volume of the reaction channel refers to the sum of each reaction channel volume, single reaction channel
Volume refer to that the feeder connection face, exit face and reaction channel inner wall are formed by the volume in space.The heat exchanger channels
Volume refer to space that reacting replacing heat area shell side inner wall, all reaction channel outer walls and connected tube sheet surface are surrounded
Volume.Since heat exchanger channels volume is much larger than reaction channel volume, reaction heat can be removed in time, guarantee that heat transfer process is stablized,
Maintain the ideal reaction time.
In multichannel microreactor provided by the utility model, at least one is equipped in the heat exchanger channels of the microreactor
A heat exchange partition 12.
The cross-sectional area of the heat exchange partition 12 is the 40~90% of the cross-sectional area of the heat exchanger channels.
Multichannel microreactor provided by the utility model, the microreactor can be horizontally arranged or place vertically.
Multichannel microreactor provided by the utility model can be used for the continuous synthesis of poly alpha olefine synthetic oil (PAO),
With high conversion rate, selective good and stable operation temperature advantage.Continuous synthesis for poly- α-olefin oil (PAO)
Operation condition are as follows: reaction pressure be 0.1~4MPa, reaction temperature be 0~100 DEG C.
1 illustrates the structure of the utility model multichannel microreactor and for continuous synthesizing poly alpha-olefin referring to the drawings
The reaction of synthetic oil.
As shown in Fig. 1, multichannel microreactor provided by the utility model successively includes distributing chamber 6, reacting replacing heat
Distributed component 13 is arranged in the distributing chamber 6 for area and collecting chamber 5, and the reacting replacing heat area is by multiple reaction channels 9 and neighbour
The heat exchanger channels 8 connect form, and hybrid component 10 is arranged in the reaction channel, is equipped with multiple heat exchange in the heat exchanger channels
Partition 12, the microreactor entrance 2 are sequentially communicated through distributing chamber 6, reaction channel 9, collecting chamber 5 and microreactor outlet 1,
Heat transferring medium entrance 4 is connected to through heat exchanger channels with heat transferring medium outlet 3.
Reaction-ure mixture is by alpha-olefin (C6~C13)、BF3(weight ratio with alpha-olefin is 0.1~4%) and alcohols object
Matter (weight ratio with alpha-olefin is 0.01~2%) composition, enters distributing chamber 6 by the micro- reaction entrance 2 of multichannel.By distribution
The effect of component 13, mixture fluid uniformly enter each reaction channel 9.Hybrid component 10 is equipped with inside reaction channel 9, it can
With the mixing and reaction process of fortified mixture.The mixture fluid for completing reaction enters collecting chamber 5, finally by reaction outlet 1
Reactor is discharged.Heat transferring medium enters heat exchanger channels, and the multiple baffling of generation of the effect in heat exchange partition by heat exchange entrance 4,
Reactor is finally left by heat exchange outlet 3.The heat released in reaction process takes away reactor by heat transferring medium.
The operating condition of the reaction of continuous synthesizing poly alpha-olefin synthetic oil be 0.1~4MPa of reaction pressure, preferably 0.5~
3MPa, reaction temperature are 0~100 DEG C, preferably 5~50 DEG C.
It is described in conjunction with the accompanying specific embodiment of the present utility model above, but the utility model is not limited to above-mentioned reality
Apply the detail in mode, in the range of the technology design of the utility model, can to the technical solution of the utility model into
The a variety of simple variants of row, these simple variants belong to the protection scope of the utility model.
The implementation method of the utility model is further illustrated by the following examples, but is not therefore limited originally practical new
Type.
Embodiment 1
Using multichannel microreactor as shown in Fig. 1.Successively include distributing chamber 6, reacting replacing heat area and collecting chamber 5,
Distributed component 13 is set in the distributing chamber 6, and the reacting replacing heat area is by multiple reaction channels 9 and adjacent heat exchanger channels
8 compositions, the reaction channel is interior to be arranged hybrid component 10, and multiple heat exchange partitions 12 are equipped in the heat exchanger channels, described
Microreactor entrance 21 be sequentially communicated through the outlet of distributing chamber 6, reaction channel 9, collecting chamber 5 and microreactor, the heat exchange
Medium inlet 4 is connected to through heat exchanger channels with heat transferring medium outlet 3.
The diameter of multichannel microreactor shell is 60mm, and length 2600mm, the length of distributing chamber 6 is 300mm, reaction
The length of heat transfer zone is 2000mm, and the length of collecting chamber is 300mm.It include 4 reaction channels in micro- reacting replacing heat area, every anti-
The cross section for answering channel is rectangle, cross-sectional area 20mm2, the length of reaction channel is 2000mm.Mixing in reaction channel
Component is cross-fin structure.The volumetric ratio of heat exchanger channels and reaction channel is 20:1.Heat exchange partition sectional area be
1300mm2。
Reaction mixture is by 1- decene, BF3It is butanol composition, wherein BF with initiator3Mass ratio with 1- decene is 3%,
The mass ratio of butanol and decene is that the inlet amount of 0.3%, 1- decene is 15g/min.Reaction mixture is entered by reactor inlet 2
Distributing chamber enters each reaction channel after distributed component is distributed.It is 25 DEG C in reaction temperature, reaction pressure is 0.6MPa's
Under the conditions of react.The mixture fluid for completing reaction enters collecting chamber, finally exports discharge reactor by reaction.Heat transferring medium by
Heat exchange entrance enters heat exchanger channels, and inlet temperature is 10 DEG C, in the multiple baffling of generation of the effect of heat exchange partition, finally by exchanging heat
Reactor is left in outlet, and outlet temperature is 16.8 DEG C.
Conversion ratio through detection reaction is 99.1%, and wherein tripolymer and the tetramer account for the 75% of product gross mass.
Claims (10)
1. a kind of multichannel microreactor, which is characterized in that it successively include distributing chamber (6), reacting replacing heat area and collecting chamber (5),
Distributed component (13) are set in the distributing chamber (6), the reacting replacing heat area is by multiple reaction channels (9) and what is abutted change
The passage of heat (8) composition, the reaction channel is interior to be arranged hybrid component (10), and the microreactor entrance (2) is through distributing chamber
(6), reaction channel (9), collecting chamber (5) and microreactor outlet (1) are sequentially communicated, and heat transferring medium entrance (4) is through heat exchanger channels
It is connected to heat transferring medium outlet (3).
2. multichannel microreactor described in accordance with the claim 1, which is characterized in that the cross section of the reaction channel (9)
Product is 1~150mm2, length is 50~5000mm, and the distance between two neighboring reaction channel (9) is 1~50mm.
3. multichannel microreactor according to claim 2, which is characterized in that the cross section of the reaction channel (9)
Product is 10~120mm2, length is 100~3000mm, and the distance between two neighboring reaction channel (9) is 3~30mm.
4. multichannel microreactor described in accordance with the claim 1, which is characterized in that the distributed component (13) has distribution
Hole or item seam.
5. multichannel microreactor described in accordance with the claim 1, which is characterized in that the hybrid component (10), which has, to intersect
Fin structure, corrugated board structures or porous media structure.
6. multichannel microreactor described in accordance with the claim 1, which is characterized in that the heat exchanger channels volume and reaction channel
Volumetric ratio be 4-30:1.
7. multichannel microreactor according to claim 6, which is characterized in that the heat exchanger channels volume and reaction channel
Volumetric ratio be 5-20:1.
8. multichannel microreactor described in accordance with the claim 1, which is characterized in that distributing chamber (6) in the microreactor,
Reacting replacing heat area and collecting chamber (5) are 1:5~20:1 along axial length ratio.
9. multichannel microreactor described in accordance with the claim 1, which is characterized in that in the heat exchanger channels of the microreactor
Partition (12) are exchanged heat equipped at least one.
10. multichannel microreactor according to claim 9, which is characterized in that the heat exchange partition (12) it is transversal
The ratio between area and the cross-sectional area of heat exchanger channels are 40~90%.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN201821064649.XU CN208975763U (en) | 2018-07-05 | 2018-07-05 | A kind of multichannel microreactor |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110860263A (en) * | 2019-12-27 | 2020-03-06 | 西部金属材料股份有限公司 | High-efficiency reactor |
| CN113522191A (en) * | 2020-04-20 | 2021-10-22 | 中国石油化工股份有限公司 | Apparatus and method for producing polyalphaolefins |
| CN118491440A (en) * | 2024-07-17 | 2024-08-16 | 西南石油大学 | Microreaction channel and microreactor |
-
2018
- 2018-07-05 CN CN201821064649.XU patent/CN208975763U/en active Active
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110860263A (en) * | 2019-12-27 | 2020-03-06 | 西部金属材料股份有限公司 | High-efficiency reactor |
| CN110860263B (en) * | 2019-12-27 | 2024-06-25 | 西部金属材料股份有限公司 | High-efficiency reactor |
| CN113522191A (en) * | 2020-04-20 | 2021-10-22 | 中国石油化工股份有限公司 | Apparatus and method for producing polyalphaolefins |
| EP4140576A4 (en) * | 2020-04-20 | 2024-08-07 | China Petroleum & Chem Corp | Device and method for preparing polyalphaolefin |
| CN118491440A (en) * | 2024-07-17 | 2024-08-16 | 西南石油大学 | Microreaction channel and microreactor |
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