CN102019158A - Tubular gas-liquid reactor capable of realizing synchronization of rotational flow and injection - Google Patents
Tubular gas-liquid reactor capable of realizing synchronization of rotational flow and injection Download PDFInfo
- Publication number
- CN102019158A CN102019158A CN 201010526062 CN201010526062A CN102019158A CN 102019158 A CN102019158 A CN 102019158A CN 201010526062 CN201010526062 CN 201010526062 CN 201010526062 A CN201010526062 A CN 201010526062A CN 102019158 A CN102019158 A CN 102019158A
- Authority
- CN
- China
- Prior art keywords
- gas
- liquid
- reactor
- injection
- spiral plate
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Images
Landscapes
- Physical Or Chemical Processes And Apparatus (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention provides a tubular gas-liquid reactor capable of realizing synchronization of rotational flow and injection, relating to chemical equipment. The tubular gas-liquid reactor capable of realizing synchronization of rotational flow and injection comprises a gas-liquid reaction tube, a gas-liquid mixing spiral element, a gas injection pipe, a jacket heat exchange tube, a liquid inflow tube and the like, wherein the gas-liquid mixing spiral element is composed of a plurality of spiral laminas, and the circumference of the gas-liquid mixing spiral element is welded on the surface of the gas injection pipe in a uniform distribution mode; the wall of the gas injection pipe is provided with a through hole, and the through hole is distributed uniformly along a spiral channel and form an included angle with the tangential plane of the gas injection pipe surface. While increasing gas-liquid contact length, gas pressure is used to push the liquid to flow, thus reducing resistance consumption of a system. The gas-liquid reactor has the advantages that the gas-liquid injection mixing and rotational flow static mixing are synchronized, the structure is simple, the operation is stable, and the mass transfer effect is good. The gas-liquid reactor is suitable for various industry fields, particularly for a reactor of which the gas-liquid flow ratio is required to be in a larger range.
Description
Technical field
The present invention relates to a kind of chemical industry equipment, particularly relate to a kind of eddy flow and spray synchronous tubular type gas-liquid reactor.
Background technology
In many chemical processes such as hydrogenation, chlorination, sulfonation, tail gas absorption, Liquid Flow, mixing and mass transfer are a kind of important modes of production.Typical gas-liquid reactor can be divided into tower reactor, tank reactor, tubular reactor and injection reactor according to its overall structures.Industrial production comprises the requirement of gas-liquid reactor: have higher production intensity; Help the raising of reaction selectivity; Help reducing energy consumption; Help the control of reaction temperature; Can under less fluid flow rate, work.Various reactors all have the scope of application and pluses and minuses separately, any reactor all can not satisfy above-mentioned requirements fully, but fully utilize the advantage of two or more reactor, reactor is carried out structure optimization, just can design the high efficiency reactor that satisfies multiple reaction requirement.Bearing capacity height, the volume of the existing tubular reactor of gas-liquid reactor of the present invention is little, specific area is big, back-mixing is few, response parameter is easy to advantages such as control, has the injection reactor compact conformation again, operates advantages such as reliable, good mixed effect and mass transfer effect.
Summary of the invention
The object of the present invention is to provide a kind of eddy flow and spray synchronous tubular type gas-liquid reactor.Can realize that Gas-Liquid Dispersion is sprayed mixing and cyclone-static mixes the tubular reactor that has screw element that carries out synchronously, this reactor has the bearing capacity height, volume is little, specific area is big, back-mixing is few, response parameter is easy to control.
The objective of the invention is to be achieved through the following technical solutions:
The tubular type gas-liquid reactor that eddy flow is synchronous with injection, include left-handed spiral plate, right hand helix plate, reach gas injection tube, gas liquid reaction pipe, chuck heat exchanger tube, liquid inflow pipe that tube wall has through hole, evenly cutting apart on the circumferencial direction of left-handed spiral plate, right hand helix plate has gas liquid reaction pipe and the formed annulus of gas injection tube; In the spiral plate quantity on the same cross section is more than 2 or 2, and its rotation direction is identical, mixed cell of formation; The spiral plate rotation direction of adjacent mixed cell is opposite, and is provided with angle at the mixed cell intersection, and its angle is half of adjacent spiral plate angle; Spiral plate is inboard to weld one with gas injection tube; Fit with the gas liquid reaction inside pipe wall in the spiral plate outside, its gap is less than 1mm; The pitch of spiral plate is 1 ~ 4 times of gas liquid reaction bore, and its torsion angle is between 90 ° ~ 270 °.
The tubular type gas-liquid reactor that described eddy flow is synchronous with injection, described injection tube wall has through hole, the helical duct that its through hole forms along the mixed cell spiral plate, spiral distribution uniformly on tube wall, through hole becomes angle with the section on gas injection tube surface, and its angle is between 30 ° ~ 90 °; Through-hole diameter is more than the 2mm; The playpipe radius wall thickness is not less than 3mm; Not perforate in back 1 ~ 3 mixed cell length range of playpipe upper edge fluid overall flow direction.
The tubular type gas-liquid reactor that described eddy flow is synchronous with injection, its described gas liquid reaction pipe diameter are that the radial height that gas sprays surpasses 1/2 of reaction tube and playpipe gap; The length of gas liquid reaction pipe is the time meter of the fluid time of staying greater than gas liquid reaction; Be connected with welding or flange between gas liquid reaction pipe and the gas dispersion playpipe.
The tubular type gas-liquid reactor that described eddy flow is synchronous with injection, the angle between described liquid inflow pipe and the gas-liquid reactor axis is not more than 90 °; Spacing between liquid inflow pipe and first hybrid element is 0.5 ~ 1.0 times of reactor diameter.
Advantage of the present invention and effect are:
1. mass-transfer efficiency height, the gas-liquid fluid disperse to spray and cyclone-static mixing synchronous effect under, gas-liquid mixed is even, and is bigger than phase contact area, the mass tranfer coefficient height;
2. bearing capacity is strong, and this gas-liquid reactor caliber is less, can bear higher gas-liquid pressure medium, can be applied to the reaction under high pressure operating mode;
3. can effectively solve the fuel factor problem of gas liquid reaction, the reactor cross section temperature is even, and reaction effect is good, and can realize the alternating temperature control along the pipe range direction;
4. alternative still formula or tower reactor are made the continuous operation type reactor;
5. fluid flows near piston flow, and no air-teturning mixed phenomenon has effectively been avoided the generation of side reaction, has improved product purity;
6. each mixed cell is convenient to maintenance and cleaning by forming an integral body with the gas injection tube welding;
7. at different application scenarios and operating condition, flexibly changing circulation passage number and gas jetting hole diameter and quantity reach optimization.
Description of drawings
Fig. 1 is hybrid element and gas injection tube assembly structure figure;
Fig. 2 is hybrid element and gas injection tube A-A cross-sectional view;
Fig. 3 is a gas-liquid injection pipe cutaway view;
Fig. 4 is the eddy flow tubular type gas-liquid reactor installation example picture synchronous with injection.
The specific embodiment
The present invention is described in detail with reference to the accompanying drawings.
Among the figure: 1 is left-handed spiral plate, and 2 is the right hand helix plate, and 3 is gas injection tube, and 4 for the gas liquid reaction pipe, and 5 be the liquid inflow pipe, and 6 be the chuck heat exchanger tube, and 7 go into (going out) for heat transferring medium mouthful manages, and 8 manage for heat transferring medium goes out (going into) mouth.
Be gas jetting hole quantity,
Be the gas jetting hole diameter,
Be gas jetting hole axis and reaction tube surface angle,
Dotted line is represented orientation, spiral plate place, the corresponding cross section of adjacent mixed cell,
Be the adjacent spiral plate angle of same mixed cell,
For the corresponding spiral plate angle in the corresponding cross section of adjacent mixed cell, generally get
Tubular reactor provided by the present invention, can form radially flow field in the flow process of gas-liquid fluid in helical duct, make the gas-liquid in the flow section distribute more even, the gas-liquid fluid is when flowing through the hybrid element interface simultaneously, the angle because adjacent mixed cell staggers, gas-liquid can be subjected to the dissection of next mixed cell spiral plate, and bigger gas group separates under the effect of shearing force, form less bubble, make than phase contact area increase, mass-transfer efficiency and improve.The gas injection tube wall has through hole, through hole evenly distributes along helical duct spiral on tube wall that the mixed cell spiral plate forms, and through hole becomes angle with section, gas injection tube surface, this angle is between 30 °～90 °, the angle of inclination is when increasing the gas-liquid contact length, utilize gas pressure to promote liquid flow, can reduce SR consumption.Through-hole diameter and quantity depend on gas flow and pressure drop requirement, say that from machining angle through-hole diameter is preferably more than the 2mm; Spraying caliber should determine according to gas flow, and wall thickness is not less than 3mm and has certain wall length to guarantee flight firm welding and inclined via-hole; Not perforate in back 1～3 mixed cell length range of playpipe upper edge fluid overall flow direction is to guarantee that all fluids all are subjected to the gas-liquid injection mixing and mix two kinds of effects with cyclone-static.Present three aspects of the acting body of gas injection tube: the one, the fixed connecting piece of spiral plate had both guaranteed axially and circumferentially locating of spiral plate, had guaranteed the location of whole hybrid element in the gas liquid reaction pipe again; The 2nd, the drainage dispersion pipe of gas, gas flows to the center of reactor by this pipe, because tube wall axially evenly has through hole circumferential reaching, gas is spread out by these through holes and the different liquid contact that circumferentially reaches axial location, has realized the dispersion mixing of gas-liquid; The 3rd, gas ejector, owing to have the less through hole of diameter on the tube wall, each through hole is equivalent to a nozzle to a certain extent, gas sprays and makes liquid dispersion become droplet, has increased the gas-liquid contact area, has strengthened mixed effect, has strengthened mass transfer.
The gas liquid reaction pipe is the space of gas-liquid mixed mass transfer, and its diameter depends on the gas-liquid flow, and its length depends on reaction speed.Under the prerequisite that satisfies the system pressure drop requirement, gas liquid reaction pipe diameter should guarantee that the radial height that gas sprays surpasses 1/2 of reaction tube and playpipe annular space.The gas liquid reaction length of tube will guarantee the fluid time of staying more than or equal to the gas liquid reaction time, should the strict relation of controlling both diameters for chain reaction.Can adopt welding or flange to be connected between gas liquid reaction pipe and the gas dispersion playpipe.Contain solid particle when liquid viscosity in the big or gas and should adopt the flange connection, so that the maintenance and the cleaning of hybrid element and gas dispersion playpipe, but answer the seal request of strict guarantee flange.Gas liquid reaction often is accompanied by heat release or heat absorption, may be strong heat release or strong heat absorption sometimes.Utilize the chuck heat exchanger tube can effectively solve the fuel factor problem of gas liquid reaction.Because the diameter (gas liquid reaction pipe diameter) generally less (usually below DN200) of tubular reactor, and the spiral hybrid element is housed in this reactor, reduced the radial symmetry gradient in Liquid Flow zone, attenuate thermal-boundary-leyer thickness, improved convection transfer rate, thereby utilize the stable control that heat transferring medium in the chuck heat exchanger tube can realization response tube fluid temperature, avoided the generation of the side reaction that causes owing to non-uniform temperature.Utilize the chuck heat exchanger tube also can realize the segmentation alternating temperature control of gas liquid reaction, be about to the chuck heat exchanger tube and be divided into several sections, each several part feeds the heat transferring medium of different temperatures (or enthalpy) just can realize the alternating temperature control of gas liquid reaction, thereby obtains different product.
The synchronous tubular type gas-liquid reactor of eddy flow of the present invention and injection can be widely used in the occasion of carrying out gas-liquid mixed and reaction continuously, is used for substituting existing stirred-tank reactor, sprays tank reactor or tower reactor.Batch reactor of the present invention can be arranged vertically, horizontally disposed, be in tilted layout; But can single use also serial or parallel connection use, serial or parallel connection can adopt butt joint or adopt tube connector to connect when using, connected mode can adopt welding or flange to connect.
Below be the example of the present invention aspect ethoxylation.
Oxirane (EO) is called ethoxylation with the reaction that many organic compounds (initiator) that contain active hydrogen carry out the open loop addition, use different initiators can obtain hundreds of products such as polyethylene glycol, non-ionic surface active agent, these ethoxylated products are very important chemical intermediate and fine chemical products in the modern industry.In view of to the vast demand of ethoxylated product and to the importance of national economy, to research, the exploitation of ethoxylation device and to improve be the major issue that EO deep processing field is paid close attention to always.Ethoxylation is the special polymerisation of a class, reacts strong heat release, and active, inflammable and explosive, the easy decomposition of reactant oxirane chemical property, poisonous is high-risk chemicals, and is very high to the security requirement of device.The ethoxylation device type of document and patent report is nearly 200 kinds at present, and wherein Buss loop reactor (VLR) and Press circulation spray reactor (STLR) are advanced at present, most widely used two kinds of reactors.The no mechanical drive disk assembly of these two kinds of reactors itself, the security that has improved reactor is all shifted out reaction heat by external heat exchanger, and has increased the gas-liquid contact area by the high velocity jet of circulation fluid, has strengthened mass transfer.The essence of Buss loop reactor and Press circulation spray reactor is that injection reactor combines with the effective of tank reactor, thereby possessed advantages such as mass-transfer efficiency height, work safety, but these two kinds of reactors also have the weakness of himself, such as the ethoxylation gas liquid reaction be semicontinuous reaction, reactor volume comparatively huge, need the additional external heat exchanger, equipment investment cost is big etc.Tubular type gas-liquid reactor of the present invention had both kept the characteristics of Buss loop reactor and Press circulation spray reactor, had overcome the defective of these two kinds of reactors again.
Tubular type gas-liquid reactor of the present invention is initiator as the ethoxylation device with phenol, carries out addition reaction with oxirane under the effect of alkali (potassium hydroxide) catalyst.Reactor diameter (gas liquid reaction pipe) is DN80mm, and length is 800mm, and the mixed cell port number is 3, and gas jetting hole quantity is 120, and diameter is 3mm, and gas jetting hole shaft angle degree is 45 °.Gas phase oxirane enters gas injection tube under self pressure effect, the liquid phase initiator enters the gas liquid reaction pipe under the effect of pump.Oxirane is under the peptizaiton of spraying the tube wall through hole, and spouting from aperture equably along circumference and axis direction, the air-flow that ejects enters liquid phase with certain angle of inclination, promotes the helical flow of liquid phase in helical duct when finishing mass transfer.Oxirane is present in the helical duct with the micro-bubble form, under the effect in the formed radially flow field of helical flow, gas-liquid distributes more even, in gas-liquid flow during through the mixed cell interface, gas-liquid particularly gas phase (bubble) under the shear action of next unit spiral plate, finish and disperse to mix, stoped the cohesion of minute bubbles simultaneously, further improved the hybrid reaction effect.Hybrid element is not only strengthened mass transfer, simultaneously can augmentation of heat transfer, and in the chuck heat exchanger tube, feed conduction oil and carry reaction heat in the reactor timely and effectively outside, reaction temperature control is more prone to.Experiment obtains water white liquid glycol phenylate product, and major constituent content is greater than 96%, and diethylene glycol (DEG) phenylate content has only 0.54%, need not to make with extra care just can use, and has greatly reduced cost.Export no bubble, oxirane has transformed substantially, and conversion ratio is more than 95%.Experimental result shows that this tubular type gas-liquid reactor has improved the space time yield of reactor, and space time yield can reach 1.5kg/ (m
3S), improve nearly 20 times than traditional still formula operation, and can obtain reliable and stable product.
Claims (4)
- Eddy flow with spray synchronous tubular type gas-liquid reactor, it is characterized in that including left-handed spiral plate (1), right hand helix plate (2), reach gas injection tube (3), gas liquid reaction pipe (4), chuck heat exchanger tube (5), liquid inflow pipe (6) that tube wall has through hole, evenly cutting apart on the circumferencial direction of left-handed spiral plate (1), right hand helix plate (2) has gas liquid reaction pipe and the formed annulus of gas injection tube; In the spiral plate quantity on the same cross section is more than 2 or 2, and its rotation direction is identical, mixed cell of formation; The spiral plate rotation direction of adjacent mixed cell is opposite, and is provided with angle at the mixed cell intersection, and its angle is half of adjacent spiral plate angle; Spiral plate is inboard to weld one with gas injection tube; Fit with the gas liquid reaction inside pipe wall in the spiral plate outside, its gap is less than 1mm; The pitch of spiral plate is 1 ~ 4 times of gas liquid reaction bore, and its torsion angle is between 90 ° ~ 270 °.
- 2. the tubular type gas-liquid reactor that eddy flow according to claim 1 is synchronous with injection, it is characterized in that described injection tube wall has through hole, the helical duct that its through hole forms along the mixed cell spiral plate, spiral distribution uniformly on tube wall, through hole becomes angle with the section on gas injection tube surface, and its angle is between 30 ° ~ 90 °; Through-hole diameter is more than the 2mm; The playpipe radius wall thickness is not less than 3mm; Not perforate in back 1 ~ 3 mixed cell length range of playpipe upper edge fluid overall flow direction.
- 3. the tubular type gas-liquid reactor that eddy flow according to claim 1 is synchronous with injection is characterized in that, described gas liquid reaction pipe diameter is that the radial height that gas sprays surpasses 1/2 of reaction tube and playpipe gap; The length of gas liquid reaction pipe is the time meter of the fluid time of staying greater than gas liquid reaction; Be connected with welding or flange between gas liquid reaction pipe and the gas dispersion playpipe.
- 4. the tubular type gas-liquid reactor that eddy flow according to claim 1 is synchronous with injection is characterized in that the angle between described liquid inflow pipe and the gas-liquid reactor axis is not more than 90 °; Spacing between liquid inflow pipe and first hybrid element is 0.5 ~ 1.0 times of reactor diameter.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201010526062 CN102019158B (en) | 2010-11-01 | 2010-11-01 | Tubular gas-liquid reactor capable of realizing synchronization of rotational flow and injection |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201010526062 CN102019158B (en) | 2010-11-01 | 2010-11-01 | Tubular gas-liquid reactor capable of realizing synchronization of rotational flow and injection |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102019158A true CN102019158A (en) | 2011-04-20 |
| CN102019158B CN102019158B (en) | 2013-06-19 |
Family
ID=43861186
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201010526062 Expired - Fee Related CN102019158B (en) | 2010-11-01 | 2010-11-01 | Tubular gas-liquid reactor capable of realizing synchronization of rotational flow and injection |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102019158B (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102989338A (en) * | 2012-12-27 | 2013-03-27 | 四川省机械研究设计院 | Spiral static mixer |
| CN103769032A (en) * | 2014-01-10 | 2014-05-07 | 安徽省化工设计院 | Novel tubular reactor |
| CN104587914A (en) * | 2013-10-31 | 2015-05-06 | 中国中化股份有限公司 | Continuous atomization-gas-liquid and liquid film-gas-liquid reactor |
| CN108031425A (en) * | 2017-11-30 | 2018-05-15 | 西安交通大学 | A kind of double tube reactor for being used to scrap TNT basic hydrolysis |
| CN110152584A (en) * | 2019-06-24 | 2019-08-23 | 中南大学 | A kind of pipeline reactor that can sufficiently react and there is self-cleaning function |
| CN112892462A (en) * | 2019-12-03 | 2021-06-04 | 中国石油集团工程股份有限公司 | Gas-liquid mixing device and isomerization system |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4009751A (en) * | 1973-11-09 | 1977-03-01 | Slovenska Vysoka Skola Technika | Method of and apparatus for high intensity heat and/or mass transfer between two or more phases |
| JPH06312126A (en) * | 1993-04-27 | 1994-11-08 | Kao Corp | Gas liquid contact device |
| CN1772873A (en) * | 2005-10-21 | 2006-05-17 | 上海理工大学 | Multi-tubular airlift reactor and its inner eddy flow field organizing method |
| CN1962035A (en) * | 2006-10-30 | 2007-05-16 | 西安交通大学 | Spray cyclone bed type gas liquid solid tri-phase reactor |
| CN201848235U (en) * | 2010-11-01 | 2011-06-01 | 沈阳化工大学 | Tube type gas-liquid reactor for synchronous swirling and jetting |
-
2010
- 2010-11-01 CN CN 201010526062 patent/CN102019158B/en not_active Expired - Fee Related
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4009751A (en) * | 1973-11-09 | 1977-03-01 | Slovenska Vysoka Skola Technika | Method of and apparatus for high intensity heat and/or mass transfer between two or more phases |
| JPH06312126A (en) * | 1993-04-27 | 1994-11-08 | Kao Corp | Gas liquid contact device |
| CN1772873A (en) * | 2005-10-21 | 2006-05-17 | 上海理工大学 | Multi-tubular airlift reactor and its inner eddy flow field organizing method |
| CN1962035A (en) * | 2006-10-30 | 2007-05-16 | 西安交通大学 | Spray cyclone bed type gas liquid solid tri-phase reactor |
| CN201848235U (en) * | 2010-11-01 | 2011-06-01 | 沈阳化工大学 | Tube type gas-liquid reactor for synchronous swirling and jetting |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102989338A (en) * | 2012-12-27 | 2013-03-27 | 四川省机械研究设计院 | Spiral static mixer |
| CN104587914A (en) * | 2013-10-31 | 2015-05-06 | 中国中化股份有限公司 | Continuous atomization-gas-liquid and liquid film-gas-liquid reactor |
| CN104587914B (en) * | 2013-10-31 | 2016-08-17 | 中国中化股份有限公司 | A kind of continuous way atomization gas-liquid, liquid film gas-liquid reactor |
| CN103769032A (en) * | 2014-01-10 | 2014-05-07 | 安徽省化工设计院 | Novel tubular reactor |
| CN108031425A (en) * | 2017-11-30 | 2018-05-15 | 西安交通大学 | A kind of double tube reactor for being used to scrap TNT basic hydrolysis |
| CN108031425B (en) * | 2017-11-30 | 2019-12-10 | 西安交通大学 | A bushing type reactor for scrapping TNT alkali hydrolysis |
| CN110152584A (en) * | 2019-06-24 | 2019-08-23 | 中南大学 | A kind of pipeline reactor that can sufficiently react and there is self-cleaning function |
| CN110152584B (en) * | 2019-06-24 | 2021-11-02 | 中南大学 | Pipeline reactor capable of fully reacting and having self-cleaning function |
| CN112892462A (en) * | 2019-12-03 | 2021-06-04 | 中国石油集团工程股份有限公司 | Gas-liquid mixing device and isomerization system |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102019158B (en) | 2013-06-19 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102019158B (en) | Tubular gas-liquid reactor capable of realizing synchronization of rotational flow and injection | |
| CN201848235U (en) | Tube type gas-liquid reactor for synchronous swirling and jetting | |
| KR102159044B1 (en) | Reactor and alkylation process using the reactor | |
| CN102358760B (en) | Stirred tank reactor | |
| CN104258796B (en) | A kind of novel high flux multi-layer helical is around pipe micro passage reaction | |
| CN205042452U (en) | Percussion flow heterogeneous reaction ware | |
| US8905080B2 (en) | Device for processing and conditioning of material transported through the device | |
| CN103212362B (en) | Conical spiral tube-type jet reactor | |
| CN102355942A (en) | Coaxial compact static mixer and use thereof | |
| CN103816822B (en) | Inner concentric tube double helix static mixer | |
| CN104338492B (en) | Multi-group layered submerged impinging steam reactor | |
| CN201482591U (en) | Gas distributor | |
| CN111841475A (en) | Novel high-speed rotary reactor | |
| EP1861197A1 (en) | Method for producing chemicals | |
| CN113332947B (en) | High flow ratio rapid mixer and annular reaction system using same | |
| CN100398191C (en) | Oscillatory flow tubular reactor of balking ring baffle | |
| CN214486841U (en) | Microreactor and parallel high-efficiency microreactor | |
| CN203564982U (en) | Mixer | |
| CN102974295A (en) | Reactor suitable for viscous material participation or generation | |
| WO2021035796A1 (en) | Pressurized fluid mixing device | |
| CN219186845U (en) | Gas-liquid-solid three-phase flow tube type spiral micro-channel reactor | |
| US8298493B2 (en) | Heat exchange apparatus | |
| CN203737130U (en) | Intra-tube concentric double-helix static mixer | |
| CN1321990C (en) | Apparatus and method for monotubular multi-spiral static mixed tube style chlorohydrination of propene for production of epoxypropane | |
| CN104226217B (en) | A kind of hypergravity microchannel reactor |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20130619 Termination date: 20151101 |
|
| EXPY | Termination of patent right or utility model |