CN1736577A - Multi-channeled micro-structured reactor - Google Patents
Multi-channeled micro-structured reactor Download PDFInfo
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- CN1736577A CN1736577A CN 200510012114 CN200510012114A CN1736577A CN 1736577 A CN1736577 A CN 1736577A CN 200510012114 CN200510012114 CN 200510012114 CN 200510012114 A CN200510012114 A CN 200510012114A CN 1736577 A CN1736577 A CN 1736577A
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- continuous phase
- phase fluid
- parallel channels
- distributor chamber
- fluid distributor
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- 239000012530 fluid Substances 0.000 claims abstract description 73
- 238000006243 chemical reaction Methods 0.000 claims abstract description 23
- 239000000203 mixture Substances 0.000 claims abstract description 9
- 238000002156 mixing Methods 0.000 claims description 18
- 229910001220 stainless steel Inorganic materials 0.000 claims description 10
- 239000010935 stainless steel Substances 0.000 claims description 10
- 239000012528 membrane Substances 0.000 claims description 9
- 238000001471 micro-filtration Methods 0.000 claims description 5
- 230000001105 regulatory effect Effects 0.000 claims 1
- 239000007788 liquid Substances 0.000 abstract description 7
- 208000012839 conversion disease Diseases 0.000 abstract description 6
- 238000012546 transfer Methods 0.000 abstract description 4
- 238000010008 shearing Methods 0.000 abstract description 3
- 238000011031 large-scale manufacturing process Methods 0.000 abstract description 2
- 239000002253 acid Substances 0.000 description 6
- 239000000126 substance Substances 0.000 description 6
- NZNMSOFKMUBTKW-UHFFFAOYSA-N cyclohexanecarboxylic acid Chemical compound OC(=O)C1CCCCC1 NZNMSOFKMUBTKW-UHFFFAOYSA-N 0.000 description 4
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 3
- 238000001311 chemical methods and process Methods 0.000 description 3
- -1 chemistry Substances 0.000 description 3
- 238000004140 cleaning Methods 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 2
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- 150000007513 acids Chemical class 0.000 description 2
- 239000003513 alkali Substances 0.000 description 2
- 229910000019 calcium carbonate Inorganic materials 0.000 description 2
- VZFUCHSFHOYXIS-UHFFFAOYSA-N cycloheptane carboxylic acid Natural products OC(=O)C1CCCCCC1 VZFUCHSFHOYXIS-UHFFFAOYSA-N 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000002283 diesel fuel Substances 0.000 description 2
- 239000003814 drug Substances 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000009776 industrial production Methods 0.000 description 2
- 238000000034 method Methods 0.000 description 2
- 239000003208 petroleum Substances 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- XTZPGMATVKNVEX-UHFFFAOYSA-N CCCCCC.OC(=O)C1CCCCC1 Chemical compound CCCCCC.OC(=O)C1CCCCC1 XTZPGMATVKNVEX-UHFFFAOYSA-N 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 239000002270 dispersing agent Substances 0.000 description 1
- 239000008246 gaseous mixture Substances 0.000 description 1
- 238000010348 incorporation Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
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Abstract
Disclosed is amultichannel reactor with microstructure. Continuous phase inlet pipe and distribution chamber, discontinuous phase inlet pipe and distribution chamber, mixture phase buffer chamber and fluid outlet pipe connects separately, and they compose the lower cavity. Porous distribution medium is sealed in the upper distribution chamber of discontinuous phase. A parallel channel plate of continuous phase is located above the lower cavity and the upper is sealed. The continuous phase liquid flows into the reactor from the distribution chamber of inlet pipe; the discontinuous liquid flows into the parallel channel of continuous phase following through the distribution medium, distributes into minute drop or air bubble with the floating shearing force of continuous phase liquid, and then connects with the continuous phase liquid to realize the rapid mixture and reaction of the two- phase liquid; then the liquid flows out of the reactor. With the invention, the area of mass transfer is big, the reaction conversion rate is high, and large scale production can be realized.
Description
Technical field
The present invention relates to a kind of high-performance reactor that is used for rapid mixing and reaction between the chemical process fluid, particularly a kind of multi-channeled micro-structured reactor that is used to realize two kinds of fluid rapid mixing and reaction belongs to chemical process rapid mixing and consersion unit
Technical field.
Background technology
In the reaction and the separation process of various fields, particularly chemical such as chemistry, chemical industry, petrochemical industry, medicine and food, all need to carry out the mixing and the reaction of two strands or multiply storeroom, mixed performance has very important influence to course of reaction.Consersion unit commonly used has continuous stir reactor and piston flow reactor etc., and their treating capacities are big, can satisfy the large-scale industrial production requirement, but it is bad to exist mixed effect, the shortcoming that equipment volume is big and the time of staying is long.In recent years, continuous development along with the micro element process technology, software engineering researchers invent various novel micro passage reactions, they have good mixing effect, the time of staying is short, conversion ratio is high, selectivity is good, energy consumption is low and safe advantage, have been subjected to paying close attention to widely.But micro passage reaction only is applicable to the material system of cleaning owing to the restriction of size; Their treating capacity is little, can't satisfy the large-scale production of chemical process; And the processing cost costliness, the equipment cost height, these have all limited them and have been applied to the large-scale industrial production process.Therefore, a kind of high-performance reactor in conjunction with good mixing effect between fluid and the big characteristics for the treatment of capacity of exploitation has great significance to the reaction and the separation process of chemical.
Summary of the invention
The objective of the invention is to propose a kind of novel high-performance reactor, i.e. multi-channeled micro-structured reactor.It combines good mixing effect and the big characteristics for the treatment of capacity between fluid, and it is simple to have a device structure, and cost is low; Good mixing effect, the time of staying is short, reaction conversion ratio is high; Selectivity is good; Big and the advantage of low energy consumption for the treatment of capacity.
A kind of multi-channeled micro-structured reactor, it comprises the continuous phase fluid inlet tube, the continuous phase fluid distributor chamber, the dispersed phase fluid inlet tube, the dispersed phase fluid distributor chamber, mix the phase surge chamber, the mixed phase fluid outlet, the porous decentralized medium, continuous phase parallel channels plate, nine parts such as stainless steel cover plate, wherein continuous phase inlet tube and continuous phase fluid distributor chamber communicate, decentralized photo inlet tube and dispersed phase fluid distributor chamber communicate, mixing phase surge chamber and mixed phase fluid outlet communicates, the porous decentralized medium is sealed in dispersed phase fluid distributor chamber top, and they form the lower chambers of this reactor jointly; Continuous phase parallel channels plate is layered on the top of lower chambers as fluid flowing passage, it contains a series of equally distributed continuous phase parallel channels, and parallel channels and continuous phase fluid distributor chamber and mix mutually that surge chamber communicates, and separate by porous decentralized medium and dispersed phase fluid distributor chamber; The top of parallel channels seals with the stainless steel cover plate.
The present invention adopts micro-filtration membrane or porous filter medium as the medium that disperses mutually, and the film that is adopted is inoranic membrane or organic film, and the type of film is tubular film or flat sheet membrane, and the aperture is 0.1～100 micron; The width of each parallel channels with highly can regulate according to different courses of reaction, can also require to change the quantity of parallel channels according to the treating capacity of production process; Design has continuous phase and dispersed phase fluid distributor chamber, guarantees that with this flow of fluid in each passage is basic identical; Design has the phase of mixing surge chamber, stablizes to guarantee to flow in the reactor; Dispersed phase fluid form with fine droplet or bubble under the effect of pressure reduction enters in the continuous phase by decentralized medium during operation, realizes rapid mixing and reaction, and decentralized photo and continuous phase is outflow reactor together; The optimum operation of continuous phase and decentralized photo is in a ratio of 1: 100～and 100: 1.
Decentralized photo and continuous phase fluid enter reactor from continuous phase inlet tube and decentralized photo inlet tube respectively during operation under the conveying of fluid pump, and continuous phase fluid flows in each parallel channels equably through the continuous phase fluid distributor chamber; Because the dispersed phase fluid pump pressure is greater than the continuous phase fluid pump, decentralized photo passes decentralized medium by the dispersed phase fluid distributor chamber with certain flow and enters in the continuous phase parallel channels, under the effect of the mobile shearing force of continuous phase fluid, be dispersed into fine droplet or bubble, contact with continuous phase fluid, and continuous phase along the decentralized medium surface with in the flowing of certain flow, realize that two-phase mixes, and flow along decentralized medium surface together, mix and react; By mixing phase surge chamber and mixed phase fluid outlet outflow reactor, realize rapid mixing and reaction between two-phase fluid afterwards.
The present invention can be applicable to the reaction and the separation process of various fields, particularly chemical such as chemistry, chemical industry, petrochemical industry, medicine and food, and dispersant liquid drop or bubble diameter are little, are in micron order, and mass transfer area is big, the mass-transfer efficiency height, and the required time of staying is short; When incorporation time during greater than 1 second, reaction conversion ratio is all more than 95%; For the system that side reaction is arranged, good reaction selectivity is more than 90%; With pressure is motive force, and pressure reduction is in hundreds of kPa, and simple to operate, operating cost is low; Regulate the width of each parallel channels and can accomplish scale production with height and parallel access volume, the device processes amount is big; Equipment is simple, and cost of equipment is low, is the consersion unit of a kind of novel, efficient, high selectivity, low energy consumption and format high throughput.
Description of drawings
Fig. 1 is the multi-channeled micro-structured reactor structural representation, 1-continuous phase fluid inlet tube wherein, 2-continuous phase fluid distributor chamber, 3-dispersed phase fluid inlet tube, 4-dispersed phase fluid distributor chamber, 5-mixes the phase surge chamber, 6-mixed phase fluid outlet, 7-porous decentralized medium, 8-continuous phase parallel channels plate plate, 9-stainless steel cover plate.
Fig. 2 is the schematic diagram of continuous phase continuous phase parallel channels plate in the multi-channeled micro-structured reactor, wherein, and the 10-parallel channels.
The specific embodiment
With embodiment the present invention is further specified below.Embodiment is for the present invention rather than restriction the present invention are described.
Fig. 1 is the multi-channeled micro-structured reactor structural representation, 1 continuous phase fluid inlet tube wherein, 2 continuous phase fluid distributor chambers, 3 dispersed phase fluid inlet tubes, 4 dispersed phase fluid distributor chambers, 5 mix the phase surge chamber, 6 mixed phase fluid outlets, 7 porous decentralized media, 8 continuous phase parallel channels plate plates, 9 stainless steel cover plates.Continuous phase inlet tube 1 and continuous phase fluid distributor chamber 2 communicate, decentralized photo inlet tube 3 and dispersed phase fluid distributor chamber 4 communicate, mixing phase surge chamber 5 and mixed phase fluid outlet 6 communicates, porous decentralized medium 7 is sealed in dispersed phase fluid distributor chamber top, and they form the lower chambers of this reactor jointly; The top that continuous phase parallel channels plate 8 is layered on lower chambers is as fluid flowing passage, and the top of continuous phase parallel channels plate 8 seals with stainless steel cover plate 9.Decentralized photo and continuous phase fluid enter reactor from continuous phase inlet tube 1 and decentralized photo inlet tube 3 respectively during operation under the conveying of fluid pump, and continuous phase fluid flows in each parallel channels 10 equably through continuous phase fluid distributor chamber 2; Because the dispersed phase fluid pump pressure is greater than the continuous phase fluid pump, decentralized photo passes decentralized medium 7 by dispersed phase fluid distributor chamber 4 with certain flow and enters in the continuous phase parallel channels plate 8, under the effect of the mobile shearing force of continuous phase fluid, be dispersed into fine droplet or bubble, contact with continuous phase fluid, and continuous phase along the decentralized medium surface with in the flowing of certain flow, realize that two-phase mixes, and flow along decentralized medium surface together, mix and react; By mixing phase surge chamber 5 and mixed phase fluid outlet 6 outflow reactors, realize rapid mixing and reaction between two-phase fluid afterwards.
Fig. 2 is the schematic diagram of continuous phase parallel channels plate in the multi-channeled micro-structured reactor, and 10 is parallel channels.The width of each parallel channels with highly can regulate according to different courses of reaction; Can also require to change the quantity of parallel channels according to the treating capacity of production process.
Embodiment 1
The soda bath of employing 4% is a decentralized photo, the gasoline of petroleum acids content 2.061 mgKOH/g is continuous phase, with 10 microns stainless steel porous medias is decentralized medium, in containing the micro-structured reactor of 10 parallel channels, continuous phase parallel channels plate reacts depickling, (the continuous phase volume flow: the decentralized photo volume flow) be at 20: 1 o'clock, acid removal rate is 98%, and the acid number after the alkali cleaning is less than 0.04mgKOH/g comparing, the gasoline treating capacity can reach 320L/h, and each passage treating capacity is 32L/h.
The soda bath of employing 4% is a continuous phase, the diesel oil of petroleum acids content 1.455mgKOH/g is decentralized photo, with 20 microns stainless steel micro-filtration membrane is decentralized medium, in the micro-structured reactor that contains 20 parallel channels, mix depickling, (the decentralized photo flow: the continuous phase flow) be at 30: 1 o'clock, acid removal rate is 93%, and the acid number after the alkali cleaning is less than 0.06mgKOH/g comparing, the diesel oil treating capacity can reach 4000L/h, and each passage treating capacity is 200L/h.
The employing oleum is a decentralized photo, 10% cyclohexane-carboxylic acid hexane solution is a continuous phase, with 1 micron stainless steel micro-filtration membrane is decentralized medium, prepared in reaction cyclohexane acid anhydrides in the micro-structured reactor that contains 5 parallel channels, comparing (continuous phase flow: the decentralized photo flow) be at 50: 1 o'clock, remaining cyclohexane-carboxylic acid concentration in the hexane solution behind the assaying reaction, try to achieve with the cyclohexane-carboxylic acid is that the reaction conversion ratio of benchmark is 85%, selectivity is 99%, the continuous phase flow is 20L/h, and each passage treating capacity is 4L/h.
Adopt CO
2Gaseous mixture (CO with nitrogen
2Volumetric concentration is 30%) be decentralized photo, Ca (OH)
2The aqueous solution be continuous phase, nickel film with 0.2 μ m is a decentralized medium, hybrid reaction prepares calcium carbonate superfine powder in the micro-structured reactor that contains 100 parallel channels, after reaction finishes, transmission electron microscope photo shows that the diameter of the nano-calcium carbonate particles that generates is 20nm, be shaped as cube, reaction conversion ratio 100%, CO
2Utilization rate 83.7%, continuous phase flow are 3000L/h, and each passage treating capacity is 30L/h.
Cost of the present invention is low, and mass transfer area is big, and treating capacity is big, and is simple to operate, the reaction conversion ratio height; Being particularly suitable for chemical hybrid reaction field uses.
Claims (5)
1, a kind of multi-channeled micro-structured reactor, it is characterized in that this reactor comprises continuous phase fluid inlet tube, continuous phase fluid distributor chamber, dispersed phase fluid inlet tube, dispersed phase fluid distributor chamber, mixes phase surge chamber, mixed phase fluid outlet, porous decentralized medium, continuous phase parallel channels plate, nine parts of stainless steel cover plate;
Continuous phase inlet tube and continuous phase fluid distributor chamber communicate, decentralized photo inlet tube and dispersed phase fluid distributor chamber communicate, mixing phase surge chamber and mixed phase fluid outlet communicates, dispersed phase fluid distributor chamber top is empty, the porous decentralized medium is sealed in dispersed phase fluid distributor chamber top, and continuous phase inlet tube, continuous phase fluid distributor chamber, decentralized photo inlet tube, dispersed phase fluid distributor chamber, mixing phase surge chamber, mixed phase fluid outlet are formed the lower chambers of this reactor jointly;
Continuous phase parallel channels plate is layered on the top of lower chambers as fluid flowing passage, it contains a series of equally distributed continuous phase parallel channels, and each parallel channels and continuous phase fluid distributor chamber and mix mutually that surge chamber communicates, it and dispersed phase fluid distributor chamber are separated by the porous decentralized medium; The top of parallel channels seals with the stainless steel cover plate.
2, a kind of multi-channeled micro-structured reactor according to claim 1 is characterized in that, described porous decentralized medium is micro-filtration membrane or porous filter medium.
3, a kind of multi-channeled micro-structured reactor according to claim 1, it is characterized in that, contain a series of equally distributed continuous phase parallel channels on the described continuous phase parallel channels plate, the width of continuous phase parallel channels is regulated according to different courses of reaction with height.
4, a kind of multi-channeled micro-structured reactor according to claim 2 is characterized in that, the micro-filtration membrane film that is adopted is inoranic membrane or organic film, and the type of film is tubular film or flat sheet membrane, and the aperture is 0.1～100 micron.
5, a kind of multi-channeled micro-structured reactor according to claim 1 is characterized in that, this reactor contains a plurality of continuous phase parallel channels plates.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2005100121149A CN1326605C (en) | 2005-07-08 | 2005-07-08 | Multi-channeled micro-structured reactor |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2005100121149A CN1326605C (en) | 2005-07-08 | 2005-07-08 | Multi-channeled micro-structured reactor |
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| CN1736577A true CN1736577A (en) | 2006-02-22 |
| CN1326605C CN1326605C (en) | 2007-07-18 |
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103007574A (en) * | 2012-12-25 | 2013-04-03 | 西安建筑科技大学 | Liquid membrane extraction method by taking hollow fiber composite membrane as liquid membrane carrier |
| CN106334505A (en) * | 2016-10-31 | 2017-01-18 | 山东豪迈化工技术有限公司 | Multiphase flow hybrid-reaction channel and microreactor |
| CN108164460A (en) * | 2018-01-12 | 2018-06-15 | 清华大学 | A kind of method for preparing 3- methylpyridine N oxides |
| CN108553939A (en) * | 2018-05-31 | 2018-09-21 | 昆明理工大学 | A kind of 3D printing multi-pore channel microreactor and its application |
| CN109836334A (en) * | 2019-02-14 | 2019-06-04 | 清华大学 | A method of continuously preparing cyclopropylamine |
| CN113104875A (en) * | 2021-03-31 | 2021-07-13 | 陕西金禹科技发展有限公司 | Process for preparing superfine or nano calcium carbonate from carbide slag and treatment system thereof |
| WO2022266952A1 (en) * | 2021-06-24 | 2022-12-29 | 山东清创化工有限公司 | Micro-reaction apparatus and method for preparing biodiesel by base catalysis |
| CN115591496A (en) * | 2022-10-24 | 2023-01-13 | 贵州大学（Cn） | Micro-reaction equipment for preparing nano lithium aluminum titanium phosphate and using method |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101234324B (en) * | 2007-11-21 | 2010-06-09 | 清华大学 | Micro-contact mixer |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB2359765B (en) * | 2000-03-02 | 2003-03-05 | Univ Newcastle | Capillary reactor distribution device and method |
| KR100845200B1 (en) * | 2001-05-07 | 2008-07-10 | 유오피 엘엘씨 | Apparatus for mixing and reacting at least two fluids |
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2005
- 2005-07-08 CN CNB2005100121149A patent/CN1326605C/en active Active
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103007574A (en) * | 2012-12-25 | 2013-04-03 | 西安建筑科技大学 | Liquid membrane extraction method by taking hollow fiber composite membrane as liquid membrane carrier |
| CN103007574B (en) * | 2012-12-25 | 2015-01-07 | 西安建筑科技大学 | Liquid membrane extraction method by taking hollow fiber composite membrane as liquid membrane carrier |
| CN106334505A (en) * | 2016-10-31 | 2017-01-18 | 山东豪迈化工技术有限公司 | Multiphase flow hybrid-reaction channel and microreactor |
| CN106334505B (en) * | 2016-10-31 | 2019-04-19 | 山东豪迈化工技术有限公司 | A kind of multiphase flow hybrid reaction channel and microreactor |
| CN108164460A (en) * | 2018-01-12 | 2018-06-15 | 清华大学 | A kind of method for preparing 3- methylpyridine N oxides |
| CN108164460B (en) * | 2018-01-12 | 2020-09-22 | 清华大学 | Method for preparing 3-methylpyridine-N-oxide |
| CN108553939A (en) * | 2018-05-31 | 2018-09-21 | 昆明理工大学 | A kind of 3D printing multi-pore channel microreactor and its application |
| CN109836334A (en) * | 2019-02-14 | 2019-06-04 | 清华大学 | A method of continuously preparing cyclopropylamine |
| CN113104875A (en) * | 2021-03-31 | 2021-07-13 | 陕西金禹科技发展有限公司 | Process for preparing superfine or nano calcium carbonate from carbide slag and treatment system thereof |
| WO2022266952A1 (en) * | 2021-06-24 | 2022-12-29 | 山东清创化工有限公司 | Micro-reaction apparatus and method for preparing biodiesel by base catalysis |
| CN115591496A (en) * | 2022-10-24 | 2023-01-13 | 贵州大学（Cn） | Micro-reaction equipment for preparing nano lithium aluminum titanium phosphate and using method |
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| Publication number | Publication date |
|---|---|
| CN1326605C (en) | 2007-07-18 |
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Assignee: Zhejiang Xinhui Synthetic New Materials Co.,Ltd. Assignor: Tsinghua University Contract record no.: 2011330000919 Denomination of invention: Multi-channeled micro-structured reactor Granted publication date: 20070718 License type: Exclusive License Open date: 20060222 Record date: 20110708 |