CN101757881A - Continuous reacting device and method for strong exothermic reaction - Google Patents
Continuous reacting device and method for strong exothermic reaction Download PDFInfo
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- CN101757881A CN101757881A CN200810207680A CN200810207680A CN101757881A CN 101757881 A CN101757881 A CN 101757881A CN 200810207680 A CN200810207680 A CN 200810207680A CN 200810207680 A CN200810207680 A CN 200810207680A CN 101757881 A CN101757881 A CN 101757881A
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- 238000006243 chemical reaction Methods 0.000 title claims abstract description 193
- 238000000034 method Methods 0.000 title claims abstract description 40
- 239000000463 material Substances 0.000 claims description 24
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 230000007423 decrease Effects 0.000 abstract 1
- ZMXDDKWLCZADIW-UHFFFAOYSA-N N,N-Dimethylformamide Chemical compound CN(C)C=O ZMXDDKWLCZADIW-UHFFFAOYSA-N 0.000 description 9
- 239000012071 phase Substances 0.000 description 9
- 230000008569 process Effects 0.000 description 9
- 238000005516 engineering process Methods 0.000 description 7
- 239000011259 mixed solution Substances 0.000 description 6
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 description 6
- GOYDNIKZWGIXJT-UHFFFAOYSA-N 1,2-difluorobenzene Chemical compound FC1=CC=CC=C1F GOYDNIKZWGIXJT-UHFFFAOYSA-N 0.000 description 5
- 239000007791 liquid phase Substances 0.000 description 5
- CETVQRFGPOGIQJ-UHFFFAOYSA-N lithium;hexane Chemical compound [Li+].CCCCC[CH2-] CETVQRFGPOGIQJ-UHFFFAOYSA-N 0.000 description 5
- WYURNTSHIVDZCO-UHFFFAOYSA-N Tetrahydrofuran Chemical compound C1CCOC1 WYURNTSHIVDZCO-UHFFFAOYSA-N 0.000 description 4
- 238000001816 cooling Methods 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- CKKZHJUAVRZTKF-UHFFFAOYSA-N C=O.FC1=C(C=CC=C1)F Chemical compound C=O.FC1=C(C=CC=C1)F CKKZHJUAVRZTKF-UHFFFAOYSA-N 0.000 description 3
- 125000000118 dimethyl group Chemical group [H]C([H])([H])* 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 230000035484 reaction time Effects 0.000 description 3
- 238000005057 refrigeration Methods 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- MPXDAIBTYWGBSL-UHFFFAOYSA-N 2,4-difluoro-1-methylbenzene Chemical group CC1=CC=C(F)C=C1F MPXDAIBTYWGBSL-UHFFFAOYSA-N 0.000 description 2
- NGNBDVOYPDDBFK-UHFFFAOYSA-N 2-[2,4-di(pentan-2-yl)phenoxy]acetyl chloride Chemical compound CCCC(C)C1=CC=C(OCC(Cl)=O)C(C(C)CCC)=C1 NGNBDVOYPDDBFK-UHFFFAOYSA-N 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- WKBOTKDWSSQWDR-UHFFFAOYSA-N Bromine atom Chemical compound [Br] WKBOTKDWSSQWDR-UHFFFAOYSA-N 0.000 description 2
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 2
- ZALMZWWJQXBYQA-UHFFFAOYSA-N [N].[Cl] Chemical compound [N].[Cl] ZALMZWWJQXBYQA-UHFFFAOYSA-N 0.000 description 2
- GDTBXPJZTBHREO-UHFFFAOYSA-N bromine Substances BrBr GDTBXPJZTBHREO-UHFFFAOYSA-N 0.000 description 2
- 229910052794 bromium Inorganic materials 0.000 description 2
- 239000007795 chemical reaction product Substances 0.000 description 2
- 229910052801 chlorine Inorganic materials 0.000 description 2
- 239000000460 chlorine Substances 0.000 description 2
- 238000010924 continuous production Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 229910017464 nitrogen compound Inorganic materials 0.000 description 2
- 125000001979 organolithium group Chemical group 0.000 description 2
- 238000004886 process control Methods 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 239000000376 reactant Substances 0.000 description 2
- 238000010923 batch production Methods 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 239000012847 fine chemical Substances 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000003541 multi-stage reaction Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- NHDHVHZZCFYRSB-UHFFFAOYSA-N pyriproxyfen Chemical compound C=1C=CC=NC=1OC(C)COC(C=C1)=CC=C1OC1=CC=CC=C1 NHDHVHZZCFYRSB-UHFFFAOYSA-N 0.000 description 1
- 230000009257 reactivity Effects 0.000 description 1
- 239000003507 refrigerant Substances 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 238000007039 two-step reaction Methods 0.000 description 1
- 230000003313 weakening effect Effects 0.000 description 1
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention relates to continuous reacting device and method for strong exothermic reaction. The reacting device comprises a first heat exchange device and a second heat exchange device, wherein the first heat exchange device is used for the exothermic stage of the reaction, and the second heat exchange device is used for other reaction stages of the reaction. By specially arranging the heat exchange devices for the exothermic stage of the exothermic reaction, the reacting device enhances the selectivity and yield rate of the reaction, decreases the energy consumption, and eliminates the safety hazard of dangerous maters in reaction.
Description
Technical field
The present invention relates to a kind of chemical reaction control, particularly relate to a kind of reaction unit and method that is used for strong exothermal reaction.
Background technology
At chemical field, especially in field of fine chemical, many strong exothermal reactions are arranged, as quick liquid phase reactor and liquid phase reactor extremely fast.This class reaction all has the very high material of one or several reactivities to participate in usually, discharges a large amount of heats in course of reaction in the short time.If the reaction liberated heat can not in time remove, reaction temperature will significantly raise, and cause required reaction not continue, and accessory substance increases.Many strong exothermal reactions need carry out under lower temperature usually, and for example subzero 78 ℃ etc., the rising of temperature of reaction system may cause required reaction not carry out in the course of reaction.In addition, the gathering of heat can make the reaction mass hot-spot, has not only reduced reaction selectivity and productive rate, and potential safety hazard also increases thereupon.
Under batch reaction conditions, strong exothermal reaction is normally undertaken by the mode of dropwise reaction material.Though this method can be controlled reaction process, reduce liberated heat at short notice, the reaction time is longer, and reaction temperature still is difficult to accurate control, and material hot-spot phenomenon also is difficult to avoid.CN2497861 has disclosed a kind of batch (-type) low-temperature reactor, and it comprises a refrigeration system that is arranged in the retort, by the liquid nitrogen control reaction temperature of this refrigeration system chuck of flowing through.This reaction unit utilizes its refrigeration system that the temperature of reactor has been reduced to the low temperature that general batch reactor is difficult to realize; but still can't overcome the shortcoming of batch reactor; for example reaction time is long; can't produce continuously; local temperature still is difficult to effectively control etc. in the reaction system; especially when the extremely fast strong heat release liquid phase reactor that the reactant of handling chlorine, bromine, chlorine nitrogen compound, organolithium or this class high reaction activity of acid chloride is participated in; it still can't in time remove a large amount of reaction heat, and is still very difficult to the control of reaction temperature.In addition, if do not increase new reactor, intermittent reaction technology also is difficult to enhance production capacities.
US6207835 disclosed a kind of prepare the arylide compound and with the continuous process of electrophilicity reagent reacting, this technical process adopts micro-mixer to mix the material of crossing through precooling treatment, the reaction channel via the heat exchanger heat exchange reacts then.Though react for majority, the reaction effect of this continuous processing is better than intermittent reaction technology, but this invention does not disclose how to remove a large amount of reaction heat that extremely fast exothermic reaction produces at short notice, thereby not have solution owing to can not in time removing relevant issues such as security that reaction heat brings and reaction efficiency yet.
The existing batch process that is used for strong exothermal reaction is long reaction time, and reaction selectivity is low, and productive rate is low, and energy consumption is big, and has shortcomings such as potential safety hazard, and does not still have effective continuous process at present.Therefore, need provide a kind of serialization that is applicable to carry out the reaction unit and the method for strong exothermal reaction.
Summary of the invention
The purpose of this invention is to provide a kind of reaction unit that is used for strong exothermal reaction.
According to one embodiment of present invention, the continuous reacting device that is used for strong exothermal reaction provided by the present invention comprises first heat-exchanger rig of a strong exothermic phase that is used for described reaction and second heat-exchanger rig of other stages of reaction that are used for described reaction.
Another object of the present invention provides a kind of reaction method that is used for strong exothermal reaction.
According to another embodiment of the invention, the continuous reaction method that is used for strong exothermal reaction provided by the present invention comprises step: with one first heat-exchanger rig to the strong exothermic phase heat exchange of described reaction with other stage of reaction heat exchange of one second heat-exchanger rig to described reaction.
Described heat-exchanger rig can be little heat exchanger or conventional heat exchanger.
The continuous reacting device that is used for strong exothermal reaction provided by the present invention can also comprise a mixing arrangement, is used for the hybrid reaction material.The preferred micro mixing device of described mixing arrangement comprises valve formula, labyrinth or stacked micro-mixer.Described little heat exchanger can be for carrying out heat exchange in little mixing apparatus and the reaction that the little reaction channel that reacts carries out.
The continuous reaction method that is used for strong exothermal reaction provided by the present invention also comprises step: the hybrid reaction material.
Reaction unit of the present invention can also comprise a pre-cooler, is used for reaction mass is carried out precooling.Reaction method of the present invention can also comprise a precooling step, is used for reaction mass is carried out precooling.
Compared to existing technology, continuous reacting device provided by the present invention and method reaction selectivity height, the productive rate height, constant product quality, energy consumption is low, and is safe in utilization, is easy to enhance production capacities, and is particularly useful for having the low temperature strong exothermal reaction of certain risk.
Description of drawings
Listed accompanying drawing is used to further describe specific embodiment disclosed by the invention and method, and this description is exemplary and nonrestrictive.
Fig. 1 is the schematic flow sheet that is used for the continuous reaction technical process of strong exothermal reaction according to one embodiment of present invention.
The specific embodiment
The strong exothermic phase that the present invention is directed to strong exothermal reaction is provided with a heat-exchanger rig especially, for the strong exothermal reaction stage provides high efficiency heat exchange, to solve fast a large amount of heat release problems of strong exothermic phase, effectively control reaction temperature, thereby solved reaction selectivity and conversion ratio problem.
Usually, the heat release of the strong exothermic phase of strong exothermal reaction is the most violent, also rapid, reaction produces a large amount of heats at short notice, and if these heats can not in time be removed, reaction temperature will significantly be raise, cause required reaction not continue, accessory substance increases, even the danger of blast is arranged, and after the strong exothermic phase of reaction, exothermic heat of reaction eases up.At the These characteristics of strong exothermal reaction, the present invention is provided with heat-exchanger rig especially for strong exothermic phase, and also is provided with corresponding heat-exchanger rig for other stages of reaction along the mobile direction of reaction mass.The strong exothermal reaction stage of the present invention can be that the mix stages at material begins, and is corresponding, for the first set heat-exchanger rig of strong exothermal reaction stage also is that relevant position from the mixed stage begins.
Reaction unit of the present invention and method are particularly useful for the low temperature strong exothermal reaction.In the low temperature strong exothermal reaction, reaction mass is through mixing after the precooling and reacting, first heat-exchanger rig provides heat exchange for the strong exothermal reaction stage, provide heat exchange with second heat-exchanger rig for other stages of reaction, the heat that will react generation accordingly according to the temperature control requirement in differential responses stage in time removes respectively, thereby the control reaction temperature makes required reaction carry out according to designing requirement.
Fig. 1 is according to an embodiment of the invention for being used for the schematic flow sheet of continuous reaction technical process of strong exothermal reaction.In embodiment as shown in Figure 1, pre-cooler 10 imported respectively by material 1 and material 2 and pre-cooler 20 is chilled to design temperature in advance.Then, two strands of materials after the precooling being sent into mixing arrangement 30 mixes.React after the mixing of materials.In the strong exothermic phase of reaction, carry out heat exchange by first heat-exchanger rig 40.Can be provided with a plurality of first heat-exchanger rigs in the strong exothermal reaction stage.Other stages of reaction after the strong heat exchange stage of reaction are carried out heat exchange by second heat-exchanger rig 50.Before stage, second heat-exchanger rig that also can comprise other is with the control reaction temperature at strong exothermal reaction.Each step of entire reaction course can be controlled by control device 60, also can control respectively.
Heat-exchanger rig of the present invention can be little heat exchanger, also can be conventional heat exchanger.Little heat exchanger claims micro-channel heat exchanger again, and its channel characteristics yardstick is in micron arrives the submillimeter range scale.Conventional heat exchanger comprises plate type heat exchanger, pipe heat exchanger etc.When adopting little reaction system, preferably adopt little heat exchanger.
The employed reaction unit of an alternative embodiment of the invention comprises a transport portion, a precooling part, a reactive moieties, a cooling segment and a control section.Transport portion comprises pump, flowmeter, Pressure gauge and valve; Precooling partly comprises heat exchanger, temperature sensor and valve; Reactive moieties comprises blender, temperature sensor, heat exchanger and valve; Cooling segment comprises control valve, temperature sensor and valve; Process control partly comprises control software and process instrument.Transport portion is connected with material inlet, reactive moieties is connected with material outlet, the external refrigerant of cooling segment, the process control part all directly links to each other with cooling segment with transport portion, precooling part, reactive moieties, by control software, process instrument and operation panel the operation overall process of device is implemented control.
Reaction unit of the present invention and method preferably adopt the micro-mixer in little reaction technology to realize mixing of one-step method or two-step method reaction synthetic, and adopt little heat exchanger in little reaction technology to realize the temperature control of the strong heat exchange stage of reaction.Because the passage of micro mixing device and little heat-exchanger rig is narrow and small, so when adopting little reaction technology, described reaction unit is applicable to the reaction system of no solid usually.
The preferred micron order of the channel size of described micro-mixer and little heat exchanger is compared with traditional batch reactor, has bigger specific area and littler volume.Because micro-mixer and little heat exchanger specific area height, volume is little, has good heat-conducting, so can control reaction temperature quickly and accurately.
Reacting replacing heat of the present invention part is preferred but be not limited to use stainless steel material, also can select the material of the heat exchanging part of unlike material according to the specific (special) requirements of reaction for the special reaction system.
Reaction unit of the present invention and method can realize the very interior reaction of wide temperature range.An advantage of described reaction unit and method is embodied in low-temp reaction, as the reaction below-40 ℃, reactant activity height under this condition, heat release is violent, conventional reaction unit and method are difficult to control to its reaction temperature, and apparatus and method of the present invention can be controlled reaction temperature safely, and can realize the production of serialization.
Reaction unit of the present invention and method also can be by adding the multistep reaction that realizes comprising strong exothermal reaction of pre-cooler, mixing arrangement and heat-exchanger rig etc.
Apparatus and method of the present invention are suitable for but are not limited to the liquid phase reactor that following material is participated in: chlorine, bromine, chlorine nitrogen compound or acid chloride.
Apparatus and method of the present invention are particularly useful for the low temperature liquid phase reaction of organolithium or RMgBr participation.
The preferred micro mixing device of apparatus and method of the present invention and little heat-exchanger rig can amplify production scale easily and flexibly by the number that increases micro mixing device and micro-reaction device.
Below respectively to produce adjacent difluoro toluene by hexyl lithium, o-difluoro-benzene and dimethyl suflfate and to be that example is specifically introduced the operating process of device of the present invention and the implementation process of described method by the two-step reaction that hexyl lithium, o-difluoro-benzene and dimethyl formamide are produced o-difluoro-benzene formaldehyde.
The micro-mixer of hereinafter mentioning is stacked micro-mixer, available from Bayer-EHRFELD company; Little heat exchanger is board-like little heat exchanger, available from Alfa Laval company.
Embodiment 1
O-difluoro-benzene/oxolane mixed solution with the 15wt% of 12.5kg/hr, and the mixed solution of hexyl lithium/hexane of the 33wt% of 5.0kg/hr is imported reaction unit respectively continuously, be cooled to-40 ℃ respectively through forecooler, the temperature that is about to hexyl lithium and o-difluoro-benzene drops to the required temperature of reaction respectively, imports micro-mixer then and mixes.Micro-mixer is strengthened the mixed process of two kinds of materials, mixes fully in the extremely short time of staying, and the little heat exchanger that enters then to strong heat exchange stage of reaction setting carries out strong heat exchange reaction.Because the channel size of set little heat exchanger is a micron order, specific area is very big, can remove a large amount of heats that produce in the strong exothermal reaction stage fast, so reaction temperature can be controlled at about-40 ℃.
After the of short duration strong exothermal reaction stage finished, mixtures of materials entered in the heat exchanger that is provided with into the heat exchange of remaining reaction elementary reaction.In this embodiment, the heat exchanger quantity that is provided with for the remaining reaction stage is two, and order is arranged, and according to constantly weakening of this exothermic heat of reaction intensity, the heat exchanger of corresponding exchange capability of heat is set, and material has been reacted completely when flowing out last heat exchanger.
Product that this step reaction back produces and flow are that the dimethyl suflfate that is pre-chilled to-40 ℃ 40wt%/oxolane mixed solution of 6.7kg/hr mixes in another micro-mixer, enter in two heat exchangers that another group is linked in sequence again and react, reaction temperature is controlled at-40 ℃.Reaction finishes the adjacent difluoro toluene of back output end product.Reaction selectivity is 94%.
Embodiment 2
The material that the difference of embodiment 2 and example 1 has been to change the material use amount of first step reaction and has changed the reaction of second step, and changed reaction condition accordingly.Adopt dimethyl formamide to replace dimethyl suflfate, reaction generates needed o-difluoro-benzene formaldehyde.Concrete operations are as follows:
O-difluoro-benzene/oxolane mixed solution with the 15.5wt% of 5.9kg/hr, and the mixed solution of hexyl lithium/hexane of the 33wt% of 2.4kg/hr, be cooled to-45 ℃ with pump input forecooler respectively, entering micro-mixer mixes, two conventional heat exchanger heat exchange reactions that enter little heat exchanger again, are linked in sequence, be that the dimethyl formamide that is pre-chilled to-40 ℃ 25wt%/oxolane mixed solution of 2.9kg/hr mixes at another micro-mixer with flow then, enter in two heat exchangers that another group is linked in sequence again and react, reaction temperature is controlled at-45 ℃.Reaction finishes back output end product o-difluoro-benzene formaldehyde.Reaction selectivity is 93%.
Above-mentioned two embodiment show reaction unit of the present invention and the method used, can solve the problem that a large amount of reaction heat that the strong exothermal reaction stage is emitted remove fast, thereby realize accurate control, eliminated potential safety hazard, improved reaction selectivity the strong exothermal reaction phase temperature.
Though the present invention discloses preferred embodiment as above; right its is not in order to limiting the present invention, anyly has the knack of this skill person, without departing from the spirit and scope of the present invention; when doing various changes and retouching, therefore the protection domain of invention should be as the criterion with the claim scope of applying for a patent.
Claims (13)
1. continuous reacting device that is used for strong exothermal reaction comprises first heat-exchanger rig of a strong exothermic phase that is used for described reaction and second heat-exchanger rig of other stages of reaction that are used for described reaction.
2. reaction unit according to claim 1 is characterized in that described reaction unit comprises a micro-reaction device, and described heat-exchanger rig comprises a little heat-exchanger rig.
3. reaction unit according to claim 1 is characterized in that described reaction unit comprises a micro-reaction device, and described first heat-exchanger rig comprises a little heat-exchanger rig, and described second heat-exchanger rig comprises a conventional heat-exchanger rig.
4. as reaction unit as described in claim 2 or 3, it is characterized in that described micro-reaction device comprises a micro mixing device, is used for the hybrid reaction material flow.
5. as reaction unit as described in claim 2 or 3, it is characterized in that described micro-reaction device comprises valve formula, labyrinth or stacked microchannel.
6. as reaction unit as described in the claim 1,2 or 3, it is characterized in that described reaction unit also comprises a pre-cooler.
7. as reaction unit as described in the claim 1,2 or 3, it is characterized in that described equipment also comprises a control device.
8. reaction unit according to claim 1 is characterized in that described reaction unit comprises a plurality of first heat-exchanger rig and a plurality of second heat-exchanger rigs that are used for other stages of reaction of described reaction that are used for the strong exothermic phase of described reaction.
9. a continuous reaction method that is used for strong exothermal reaction comprises step: with one first heat-exchanger rig the strong exothermic phase of described reaction is carried out heat exchange and with one second heat-exchanger rig other stages of reaction of described reaction carried out heat exchange.
10. as method as described in the claim 9, it is characterized in that described strong exothermal reaction carries out in a micro-reaction device, described heat-exchanger rig comprises a little heat-exchanger rig.
11. as method as described in the claim 10, it is characterized in that described first heat-exchanger rig comprises a little heat-exchanger rig, described second heat-exchanger rig comprises a conventional heat-exchanger rig.
12. as method as described in claim 10 or 11, it is characterized in that, also comprise step: use a micro mixing device hybrid reaction material flow.
13. as method as described in claim 10 or 11, it is characterized in that, also comprise step: reaction mass is carried out precooling with a pre-cooler.
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| CN200810207680A CN101757881A (en) | 2008-12-24 | 2008-12-24 | Continuous reacting device and method for strong exothermic reaction |
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| CN200810207680A CN101757881A (en) | 2008-12-24 | 2008-12-24 | Continuous reacting device and method for strong exothermic reaction |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104203393A (en) * | 2012-03-30 | 2014-12-10 | 通用电气公司 | Microfluidic device and a related method thereof |
Citations (4)
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|---|---|---|---|---|
| US6207835B1 (en) * | 1998-12-19 | 2001-03-27 | Merck Kgaa | Process for the preparation of arylmetal compounds and their reaction with electrophilic reagents |
| CN1907555A (en) * | 2006-07-17 | 2007-02-07 | 南京工业大学 | Composite heat exchange type micro reactor |
| US20070151451A1 (en) * | 2005-12-22 | 2007-07-05 | Rekers Dominicus M | Process for the cooling, concentration or purification of ethylene oxide |
| JP2008086887A (en) * | 2006-09-29 | 2008-04-17 | Fujifilm Corp | Emulsion and method for producing emulsion |
-
2008
- 2008-12-24 CN CN200810207680A patent/CN101757881A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6207835B1 (en) * | 1998-12-19 | 2001-03-27 | Merck Kgaa | Process for the preparation of arylmetal compounds and their reaction with electrophilic reagents |
| US20070151451A1 (en) * | 2005-12-22 | 2007-07-05 | Rekers Dominicus M | Process for the cooling, concentration or purification of ethylene oxide |
| CN1907555A (en) * | 2006-07-17 | 2007-02-07 | 南京工业大学 | Composite heat exchange type micro reactor |
| JP2008086887A (en) * | 2006-09-29 | 2008-04-17 | Fujifilm Corp | Emulsion and method for producing emulsion |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104203393A (en) * | 2012-03-30 | 2014-12-10 | 通用电气公司 | Microfluidic device and a related method thereof |
| CN104203393B (en) * | 2012-03-30 | 2017-11-03 | 通用电气公司 | Microfluidic device and its method |
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Application publication date: 20100630 |