CN101293195A - Stirring/flow-guiding multi-phase reactor - Google Patents
Stirring/flow-guiding multi-phase reactor Download PDFInfo
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- CN101293195A CN101293195A CNA2008100364568A CN200810036456A CN101293195A CN 101293195 A CN101293195 A CN 101293195A CN A2008100364568 A CNA2008100364568 A CN A2008100364568A CN 200810036456 A CN200810036456 A CN 200810036456A CN 101293195 A CN101293195 A CN 101293195A
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Abstract
The present invention provides a stirring/guide multi-phase reactor, comprising a cylindrical sealed shell, a guide cylinder, a stirring device, air inlet device and an air outlet device; wherein, the cylindrical sealed shell is provided with a material inlet and outlet device; the lower part inside the shell is provided with the guide cylinder with an external diameter smaller than the internal diameter of the shell, a clearance is left between the guide cylinder and the shell bottom; the stirring device is arranged in the clearance between the guide cylinder and the shell bottom and comprises a stirring shaft and a blade fixed on the stirring shaft; the stirring shaft passes through the shell bottom and extends out of the shell; the air inlet device is arranged on the shell bottom and/or a lateral wall and the air outlet of the air inlet device is arranged below the blade; the air outlet device is arranged on the shell top. The stirring/guide multi-phase reactor provided by the present invention, which adopts the combination of the bottom-type stirring device and the guide cylinder, only needs comparatively low energy consumption to reach and even surpass the air rate the multi-layer or single-layer stirring reactor requires a plurality of times of energy consumption. Due to short mixing period and high effective energy utilization, the reactor is suitable for various industrial processes.
Description
Technical field
The present invention relates to a kind of reactor, be specifically related to a kind of novel heterophase reactor, particularly agitating device in the reactor and the guide shell that is arranged in the reactor.
Background technology
Heterophase reactor is a kind of reactor that is widely used in the chemical industry field, in the process industrials such as, biofermentation synthetic as, oxidation synthetic at methyl alcohol, hydrogenation, sewage disposal, Fischer-Tropsch, just need use heterophase reactor.
In said heterophase reactor, reaction raw materials and product comprise gas, liquid and solid, and therefore, for such course of reaction, gas dispersion, raw material mixing, alternate transmission, solid suspension and distribution thereof etc. require quite high.At present, industrial heterophase reactor commonly used comprises multilayer mechanically stirred reactor, three phase fluidized bed, slurry bed, inner and outer ring flow reactor etc., and these reactors respectively have pluses and minuses on performance and structure.
At present, many documents and patent disclosure technology separately, disclose a kind of being oxidized in the aromatic carboxylic acids as patent ZL.89102155.8 and improved the method and apparatus that yield and product quality cut down the consumption of energy simultaneously at aromatic alkyl, relate to a kind of heterophase reactor in this method, this heterophase reactor adopts in the agitating device bottom and feeds gas methods, to improve the gas dispersion effect.But, facts have proved that the effect of this method is unsatisfactory, can't satisfy reaction needed fully, baffle plate is too narrow again, and the mixing of material is even inadequately in the reactor; The inventor discloses a kind of aromatic oxidation that is applicable at Chinese patent ZL.CN1390823A and has produced the reactor of aromatic carboxylic acids, though across-the-board regulation structure of reactor, the mixing and the dispersion effect of three-phase system significantly improve, improved the gas holdup in the reaction system, but, also have the bigger defective of power consumption.
Therefore a kind of new heterophase reactor energy-efficient, that mix of developmental research is that process industrial and branch of industry are extremely expected.
Summary of the invention
The objective of the invention is to disclose a kind of stirring/flow-guiding multi-phase reactor, to overcome the above-mentioned defective that prior art exists.
Stirring/flow-guiding multi-phase reactor of the present invention is used for reference traditional heterophase reactor structure, has proposed new structure of reactor form, mainly comprises:
A columniform airtight housing that is provided with material outlet device and liquid phase inlet device;
A guide shell that is arranged on bottom in the said housing leaves the gap between described guide shell and the housing;
One is arranged on comprising shaft and being fixed on the agitating device of the blade on the shaft between guide shell and the housing bottom, and shaft passes housing bottom;
A gas inlet device that is arranged on housing bottom or sidewall;
A gas vent device that is arranged on case top.
Stirring/flow-guiding multi-phase reactor of the present invention, take the combination of bottom entering type agitating device and guide shell, form an organic whole in conjunction with bottom shape, not only utilize agitating device but also drive liquid by density contrast inside and outside the guide shell, gas is after the gas distributor initial dispersion enters reactor, again through agitator arm shearing-crushing and liquid phase circulation turbulent flow, circulation guide functions through the guide shell inside and outside differential pressure, repeatedly disperse bubble, can improve gas effciency effectively, improve bubble size distribution and promote the liquid circulation to accelerate liquid phase and mix, adopt individual layer agitator arm energy consumption to decline to a great extent, and the circulation of guide shell accelerating liquid is installed at agitator arm top certain distance, introduce the restriction that guide shell has solved individual layer agitator arm sphere of action effectively, in H/D＞1 o'clock, also can adopt the individual layer agitator arm, enlarge sphere of action.Actual result shows, this reactor only needs can meet or exceed multilayer or the individual layer stirred reactor need consume the gas holdup that the several times energy is reached than low energy consumption, mixed effect also improves, and has shortened incorporation time, and the energy effective utilization rate significantly improves than prior art.Because agitating device is installed in reactor bottom, have advantages such as shaft weak point, stable operation, easy care maintenance, saving material.This reactor is applicable to multiple industrial process as a kind of heterophase reactor simultaneously, as the PX oxidation, and biofermentation etc., range of application is very extensive.
Description of drawings
Fig. 1 is the general structure schematic diagram of stirring/flow-guiding multi-phase reactor.
Fig. 2 is gas holdup and the power consumption result to the cold mould experiment of air-running water system.
Fig. 3 is gas holdup and the power consumption result to the cold mould experiment of air-running water system.
The specific embodiment
Referring to Fig. 1, stirring/flow-guiding multi-phase reactor of the present invention comprises:
A columniform airtight housing 1 that is provided with material outlet device 2 and liquid phase inlet device 11, preferred, liquid phase inlet device 11 is arranged on the middle part of housing 1 or below the middle part;
A guide shell 3 that is arranged on the external diameter of bottom in the said housing 1 less than housing 1 internal diameter between the bottom of described guide shell 3 and housing 1, leaves gap 10;
Comprising shaft 5 and being fixed on the agitating device of the blade 4 on the shaft 5 in gap 10 that is arranged between guide shell 3 and housing 1 bottom, described shaft 5 passes housing 1 bottom and extends to outside the housing 1;
A gas inlet device that is arranged on housing 1 bottom and/or sidewall, the gas outlet 6 of described gas inlet device is arranged on the below of described blade 4;
A gas vent device 7 that is arranged on housing 1 top.
Further, referring to Fig. 1, the external diameter of said guide shell 3 is 1/5～4/5 times of reactor 1 internal diameter;
Further, referring to Fig. 1, be provided with outer baffle 8 in said gap 10, improve gas dispersion to improve mixed effect, the width of outer baffle 8 is 1/12～1/10 times of reactor 1 internal diameter, and is preferred, is provided with 2～6 outer baffles 8, evenly is provided with; Preferably, said baffle plate adopts fluting or slit baffle plate, concrete structure such as Chinese patent 02265664.2 disclosed technology;
Further, referring to Fig. 1, be provided with Internal baffle 9 at said guide shell 3, to improve in the guide shell mixed effect and to prevent " gyroscope-like " whirlpool, the width of Internal baffle 9 is 1/12～1/10 times of guide shell 3 internal diameters, and is preferred, be provided with 2～6 Internal baffles 9, evenly be provided with; Preferably, said baffle plate adopts fluting or slit baffle plate, concrete structure such as Chinese patent 02265664.2 disclosed technology;
Further, in described guide shell 3, be provided with the Gas-Liquid Dispersion element, as silk, net, rod, thin plate etc., to improve the gas-liquid mass transfer effect;
Further, referring to Fig. 1, the gap 10 between guide shell 3 bottoms and housing 1 bottom is 1/4～1 times of reactor 1 internal diameter; Preferably, the bottom of described guide shell 3 is provided with horn mouth 301;
Further, referring to Fig. 1, the spacing between blade 4 and housing 1 bottom is 1/4～1/3 times of reactor 1 internal diameter;
Further, the diameter of said blade 4 is 1/4～1/2 times of reactor 1 internal diameter; Preferably, said blade 4 adopts aerofoil profile axial flow oar, concrete structure such as Chinese patent 92245125.7 disclosed technology;
Further, said gas inlet device is the multitube ring type gas distributor 601 that is arranged on housing 1 sidewall, and the mouth of pipe is downward, concrete structure such as Chinese patent 02265664.2 disclosed technology;
Perhaps for being arranged on the gas distributor that constitutes by distribution rings and breather pipe 602 of housing 1 bottom, breather pipe 602 numbers are 4～8, evenly be provided with along the tower center, the distribution rings diameter is 1/5～4/5 times of reactor 1 internal diameter, and the distance of the breather pipe mouth of pipe and housing 1 bottom is 0.1～0.35 times of reactor 1 internal diameter;
Preferably, the height of reactor 1 with the internal diameter ratio is: highly/and internal diameter=0.8～4.
Stirring/flow-guiding multi-phase reactor of the present invention is operation like this:
At the stirring/flow-guiding multi-phase reactor inner bottom part axial flow agitator arm is installed; Upper impeller is equipped with the structural type guide shell, the expansion pyramid type guide shell that keeps certain relative gap, guide shell can be between impeller and guide shell having certain angle, variable cross-section guide shell etc.; Four upright line of rabbet joint baffle plates are installed in the guide shell, and all gases silk, net, plate, rod etc. of distributed component such as different-diameter and shape again can be installed; Reactor bottom or sidewall are equipped with multitube ring type gas distributor.The reaction mass that will prepare in advance during operation, the charging apertures in the middle part of reactor such as solid phase product that wherein contain reactant, water, catalyst or recovery add reactor, gas is introduced into inside reactor by the gas feed device, and liquid oxidation thing and solvent medium are drawn by the material outlet device.The gas of introducing is after the gas distributor initial dispersion, at first enter agitator arm active region, bottom, being sheared broken back rises and enters in the guide shell and continue to move upward, interphase interaction forms elevated areas in the tube, induce simultaneously to form the inside and outside density contrast of guide shell, continue to drive heterogeneous fluid and enter reactor lower part impeller action district once more by the outer circulation downwards of tube.Carry out continuously and so forth, mix and solid suspension process with gas dispersion, gas-liquid mass transfer, liquid phase in the heterophase reactor simultaneously.If related reaction is a strong exothermal reaction, then need to place condenser in reactor head, make the solvent of evaporation or reactant condensation reclaim Returning reactor, incoagulable gas and water are discharged reaction system by exhaust outlet.
Adopt the stirring/flow-guiding multi-phase reactor of said structure, because the choose reasonable and the configuration of agitating device and guide shell combining structure, coupling, coordination between impeller, guide shell, reactor bottom shape, breather pipe, the baffle plate, incorporation time is shortened, gas holdup increases, and particle suspends, and what is more important, reactor can the loss-rate prior art significantly reduce, and the energy effective utilization rate improves greatly.With close industrial production condition in simulated test in, all show the good result that obtains of the present invention.
Adopt water conservancy diversion/stirred reactor of the present invention, under identical operations operating mode (comprising that dress liquid height, impeller are from low distance, impeller feature structure, operating gas velocity etc.), gas holdup that the cold mould of air-running water system is tested and power consumption result are as shown in Figures 2 and 3.
Fig. 2 is that to be provided with the stirring/flow-guiding multi-phase reactor of the present invention of individual layer blade 4 and the traditional individual layer oar heterophase reactor that is not provided with water conservancy diversion be the comparison diagram of the gas holdup under the condition of 2.4vvm (throughput of unit liquid phase volume in the per minute) at throughput.
Among Fig. 2, curve 2 representatives result of the test of the present invention, the result of the test of the heterophase reactor that is not provided with water conservancy diversion that curve 1 representative is traditional.
Fig. 3 is that to be provided with the stirring/flow-guiding multi-phase reactor of the present invention of individual layer blade 4 and the traditional double-deck oar heterophase reactor that is not provided with water conservancy diversion be the comparison diagram of the gas holdup under the condition of 2.4vvm (throughput of unit liquid phase volume in the per minute) at throughput.
Among Fig. 3, curve 3 representatives result of the test of the present invention, the result of the test of the heterophase reactor that is not provided with water conservancy diversion that curve 4 representatives are traditional.
The result shows: under equal-wattage consumption condition, the gas holdup of reactor assembly of the present invention is significantly improved; And to obtain identical gas holdup, then power demand is about about 1/5th of double-deck oar system.
Claims (10)
1. a stirring/flow-guiding multi-phase reactor is characterized in that, comprising:
A columniform airtight housing (1) that is provided with material outlet device (2) and liquid phase inlet device (11);
A guide shell (3) that is arranged on the external diameter of the interior bottom of said housing (1) less than housing (1) internal diameter between the bottom of described guide shell (3) and housing (1), leaves gap (10);
Comprising shaft (5) and being fixed on the agitating device of the blade (4) on the shaft (5) in gap (10) that is arranged between guide shell (3) and housing (1) bottom, described shaft (5) passes bottom the housing (1) and extends to outside the housing (1);
A gas inlet device that is arranged on housing (1) bottom and/or sidewall, the gas outlet of described gas inlet device is arranged on the below of described blade (4);
A gas vent device (7) that is arranged on housing (1) top.
2. stirring/flow-guiding multi-phase reactor according to claim 1 is characterized in that, the external diameter of said guide shell (3) is 1/5～4/5 times of reactor (1) internal diameter.
3. stirring/flow-guiding multi-phase reactor according to claim 1 is characterized in that, is provided with outer baffle (8) in said gap (10), and the width of outer baffle (8) is 1/16～1/10 times of reactor (1) internal diameter, is provided with 2～6 outer baffles (8).
4. stirring/flow-guiding multi-phase reactor according to claim 3 is characterized in that, outer baffle (8) adopts fluting or slit baffle plate.
5. according to each described stirring/flow-guiding multi-phase reactor of claim 1～4, it is characterized in that, be provided with Internal baffle (9) at said guide shell (3), the width of Internal baffle (9) is 1/16～1/10 times of guide shell (3) internal diameter, be provided with 2～6 Internal baffles (9), said Internal baffle (9) adopts fluting or slit baffle plate.
6. stirring/flow-guiding multi-phase reactor according to claim 5 is characterized in that, is provided with the gas-liquid contact element in described guide shell (3).
7. stirring/flow-guiding multi-phase reactor according to claim 6, it is characterized in that, gap (10) between guide shell (3) bottom and housing (1) bottom is 1/4～1 times of reactor (1) internal diameter, spacing between blade (4) and housing (1) bottom is 1/4～1/3 times of reactor (1) internal diameter, the diameter of said blade (4) is 1/4～1/2 times of reactor (1) internal diameter, and said blade (4) adopts aerofoil profile axial flow oar, turbine turbine oar and oblique leaf oar.
8. according to each described stirring/flow-guiding multi-phase reactor of claim 1～4, it is characterized in that said gas inlet device comprises the multitube ring type gas distributor (601) that is arranged on housing (1) sidewall, the mouth of pipe is downward;
Perhaps comprise the gas distributor that is arranged on housing (1) bottom by distribution rings and breather pipe (602) formation, breather pipe (602) number is 4～8, evenly be provided with along the tower center, the distribution rings diameter is 1/5～4/5 times of reactor (1) internal diameter, and the distance of the breather pipe mouth of pipe and housing (1) bottom is 0.1～0.35 times of reactor (1) internal diameter.
9. according to each described stirring/flow-guiding multi-phase reactor of claim 1～4, it is characterized in that the height of reactor (1) with the internal diameter ratio is: highly/internal diameter=0.8～4.
10. stirring/flow-guiding multi-phase reactor according to claim 9 is characterized in that, the bottom of described guide shell (3) is provided with horn mouth.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200810036456A CN100584445C (en) | 2008-04-22 | 2008-04-22 | Stirring/flow-guiding multi-phase reactor |
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| CN200810036456A CN100584445C (en) | 2008-04-22 | 2008-04-22 | Stirring/flow-guiding multi-phase reactor |
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| CN101293195A true CN101293195A (en) | 2008-10-29 |
| CN100584445C CN100584445C (en) | 2010-01-27 |
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Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102008916A (en) * | 2010-11-04 | 2011-04-13 | 北京中农普康生物科技有限公司 | Flow guide stirring device |
| CN102489238A (en) * | 2011-12-08 | 2012-06-13 | 中国石油化工股份有限公司 | Efficient gas-liquid self-mixing reactor |
| CN102049224B (en) * | 2009-10-27 | 2013-01-23 | 中国石油化工股份有限公司 | Flow field turbulator |
| CN104437329A (en) * | 2014-12-11 | 2015-03-25 | 重庆欣欣向荣精细化工有限公司 | Compound kettle type reactor |
| CN105126729A (en) * | 2015-09-04 | 2015-12-09 | 长春黄金研究院 | Air-operated paddle stirring reactor |
| CN105664763A (en) * | 2016-03-17 | 2016-06-15 | 中国市政工程华北设计研究总院有限公司 | Density-varying pneumatic mixing liquor stirring device |
| CN108315226A (en) * | 2018-03-15 | 2018-07-24 | 郭敬承 | A kind of center air lift type high-efficient biological reactor |
| CN109621873A (en) * | 2019-01-21 | 2019-04-16 | 中建安装集团有限公司 | A kind of esterification device |
| CN110586020A (en) * | 2019-09-29 | 2019-12-20 | 沧州旭阳化工有限公司 | Redistribution type reaction device |
| CN113559796A (en) * | 2021-07-01 | 2021-10-29 | 河北科技大学 | Coupling type coal powder pyrolysis and semicoke reduction CO2Apparatus and method for producing CO |
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2008
- 2008-04-22 CN CN200810036456A patent/CN100584445C/en not_active Expired - Fee Related
Cited By (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102049224B (en) * | 2009-10-27 | 2013-01-23 | 中国石油化工股份有限公司 | Flow field turbulator |
| CN102008916A (en) * | 2010-11-04 | 2011-04-13 | 北京中农普康生物科技有限公司 | Flow guide stirring device |
| CN102489238A (en) * | 2011-12-08 | 2012-06-13 | 中国石油化工股份有限公司 | Efficient gas-liquid self-mixing reactor |
| CN104437329A (en) * | 2014-12-11 | 2015-03-25 | 重庆欣欣向荣精细化工有限公司 | Compound kettle type reactor |
| CN104437329B (en) * | 2014-12-11 | 2023-02-24 | 重庆欣欣向荣精细化工有限公司 | Compound kettle type reactor |
| CN105126729A (en) * | 2015-09-04 | 2015-12-09 | 长春黄金研究院 | Air-operated paddle stirring reactor |
| CN105664763B (en) * | 2016-03-17 | 2017-12-22 | 中国市政工程华北设计研究总院有限公司 | Density transform pneumatically mixes alloy melt stirring device |
| CN105664763A (en) * | 2016-03-17 | 2016-06-15 | 中国市政工程华北设计研究总院有限公司 | Density-varying pneumatic mixing liquor stirring device |
| CN108315226A (en) * | 2018-03-15 | 2018-07-24 | 郭敬承 | A kind of center air lift type high-efficient biological reactor |
| CN109621873A (en) * | 2019-01-21 | 2019-04-16 | 中建安装集团有限公司 | A kind of esterification device |
| CN109621873B (en) * | 2019-01-21 | 2024-04-16 | 中建安装集团有限公司 | Esterification reaction device |
| CN110586020A (en) * | 2019-09-29 | 2019-12-20 | 沧州旭阳化工有限公司 | Redistribution type reaction device |
| CN113559796A (en) * | 2021-07-01 | 2021-10-29 | 河北科技大学 | Coupling type coal powder pyrolysis and semicoke reduction CO2Apparatus and method for producing CO |
| CN113559796B (en) * | 2021-07-01 | 2024-07-19 | 河北科技大学 | Coupling type pulverized coal pyrolysis and semicoke reduction CO2Apparatus and method for producing CO |
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| CN100584445C (en) | 2010-01-27 |
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