CN2841645Y - External circulation airlift membrane reactor - Google Patents
External circulation airlift membrane reactor Download PDFInfo
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- CN2841645Y CN2841645Y CNU2005200751399U CN200520075139U CN2841645Y CN 2841645 Y CN2841645 Y CN 2841645Y CN U2005200751399 U CNU2005200751399 U CN U2005200751399U CN 200520075139 U CN200520075139 U CN 200520075139U CN 2841645 Y CN2841645 Y CN 2841645Y
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- 239000012528 membrane Substances 0.000 title claims abstract description 68
- 238000005273 aeration Methods 0.000 claims abstract description 40
- 238000006243 chemical reaction Methods 0.000 claims abstract description 30
- 229910052500 inorganic mineral Inorganic materials 0.000 claims description 21
- 239000011707 mineral Substances 0.000 claims description 21
- 239000000919 ceramic Substances 0.000 claims description 9
- 230000000694 effects Effects 0.000 claims description 6
- 238000013022 venting Methods 0.000 claims description 5
- 230000008602 contraction Effects 0.000 claims description 3
- 238000009826 distribution Methods 0.000 claims description 3
- 238000012546 transfer Methods 0.000 abstract description 16
- 238000000926 separation method Methods 0.000 abstract description 12
- 230000008901 benefit Effects 0.000 abstract description 3
- 230000008878 coupling Effects 0.000 abstract description 3
- 238000010168 coupling process Methods 0.000 abstract description 3
- 238000005859 coupling reaction Methods 0.000 abstract description 3
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 238000003756 stirring Methods 0.000 abstract description 2
- 230000003321 amplification Effects 0.000 abstract 1
- 238000003199 nucleic acid amplification method Methods 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 58
- 239000007788 liquid Substances 0.000 description 30
- 238000002156 mixing Methods 0.000 description 13
- 239000007787 solid Substances 0.000 description 12
- 238000000034 method Methods 0.000 description 10
- 239000012071 phase Substances 0.000 description 9
- 230000008569 process Effects 0.000 description 8
- 238000000855 fermentation Methods 0.000 description 7
- 230000004151 fermentation Effects 0.000 description 7
- 239000012530 fluid Substances 0.000 description 7
- 238000010586 diagram Methods 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- FRXSZNDVFUDTIR-UHFFFAOYSA-N 6-methoxy-1,2,3,4-tetrahydroquinoline Chemical compound N1CCCC2=CC(OC)=CC=C21 FRXSZNDVFUDTIR-UHFFFAOYSA-N 0.000 description 3
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 238000005538 encapsulation Methods 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 238000009423 ventilation Methods 0.000 description 3
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- 238000013019 agitation Methods 0.000 description 2
- 238000007872 degassing Methods 0.000 description 2
- 238000011065 in-situ storage Methods 0.000 description 2
- 238000002347 injection Methods 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- 238000011017 operating method Methods 0.000 description 2
- 238000003825 pressing Methods 0.000 description 2
- 230000002787 reinforcement Effects 0.000 description 2
- 230000004044 response Effects 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- 241000282326 Felis catus Species 0.000 description 1
- 230000001154 acute effect Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000005842 biochemical reaction Methods 0.000 description 1
- 230000031018 biological processes and functions Effects 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
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- 238000005516 engineering process Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
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- 239000007791 liquid phase Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000010907 mechanical stirring Methods 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 150000007524 organic acids Chemical class 0.000 description 1
- 230000036284 oxygen consumption Effects 0.000 description 1
- 238000004806 packaging method and process Methods 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 230000003014 reinforcing effect Effects 0.000 description 1
- 230000035945 sensitivity Effects 0.000 description 1
- 238000010008 shearing Methods 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 238000003746 solid phase reaction Methods 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
- 238000003466 welding Methods 0.000 description 1
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Classifications
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
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- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The utility model relates to a novel membrane reactor especially relates to an outer circulation airlift membrane reactor. The reactor comprises a reactor kettle body, an air lifting pipe, an inorganic membrane element, an axial aeration head and other parts. The inorganic membrane is used as a radial gas distributor and a separator and is packaged in the external circulation gas lifting pipe and is connected with a compressed gas source and a vacuum system, so that the coupling of continuous radial aeration and continuous reaction separation is realized. The reaction realizes the respective regulation of aeration efficiency and stirring efficiency of the airlift reactor through a cross flow aeration system consisting of an axial aeration nozzle and a radial aeration membrane, so that two parameters can be optimally selected according to the specific requirements of different stages of the reaction. The reactor has the advantages of simple device, convenient operation, wide application range, high mass transfer efficiency, low energy consumption, easy amplification and the like.
Description
Technical field
The utility model relates to a kind of novel membrane reactor, thinking particularly integrated according to flow process and process intensification is developed, the outside circulation gas lift type membrane reactor of integrated cross flow film aerating system, axial aeration reinforcing film separating system, be used for relating to the reaction that contains gas-liquid biphase heterogeneous reaction and biological fermentation such as solid of gas-liquid, gas-liquid and separate, belong to chemical industry and biochemical industry equipment.
Background technology
Airlift reactor is the contact reacts device that is used for gas-liquid two-phase or gas-liquid-solid three-phase process.Generally be made up of two different pieces, only feed gas a part, vent portion is called and rises the gas parts, and another part is injecting gas not, is called to fall the liquid parts.Airlift reactor gas enters in the external phase with the form of bubble, and this external phase can be liquid or contains solid suspension.Because ventilation has produced the different fluid density difference with the two-part different gas holdups of stuffiness, this just makes the reactor inner fluid produce and circulates.Along with fluidic circulates, most of gas rises to the liquid phase surface and overflows, and the small part bubble is involved in downtake by liquid, again circulation downwards.Circulation can make all, and each obtains well blend mutually, and solid is suspended in liquid effectively, and it is good to distribute in whole reactor, obtains gas-liquid or the solid mass transfer effect of gas-liquid preferably, and airlift reactor belongs to strength stirring-type reactor.
The kind of airlift reactor is a lot, can be divided into internal circulation gas-lift type reactor and outer circulation airlift reactor two big classes by the flow circuit situation usually, but its variation is also more.The internal circulation gas-lift type reactor is generally a simple bubble tower, a built-in division plate is divided into riser and downtake two portions with tower, and other also has the airlift reactor of multistage center pipe, multicenter pipe airlift reactor, Multi-Tube Airlift Loop Reactor etc.The riser of outer circulation airlift reactor separates fully with downtake, and by connecting respectively by two place's horizontal components at the bottom of the cat head tower, enter the interior gas injection of reactor to air-lift tube, because the injection kinetic energy of gas and riser inner fluid density reduce, force the riser fluid upwards, downtake is done well-regulated circulating downwards.Thereby form good mixing and condition.The internal circulation gas-lift type reactor has gas-liquid mass transfer preferably, and the riser gas holdup is much higher than the gas holdup of downtake.Compare with interior circulation airlift reactor, outer circulation airlift reactor flow rule, resistance is little, has the dead angle hardly, simultaneously, apparent liquid velocity is bigger, turbulent flow and gas-liquid mass transfer also increase, and heat transfer property also is better than the internal circulation gas-lift type reactor, and higher cycle rate is arranged, in addition, the also more easily degassing of outer circulation airlift reactor.
Compare with other reactors, that airlift reactor has is simple in structure, shearing force is low, air feed efficient height, effectively the interface contact area is big, fluid effect is splendid, each all has the clear and definite residence time and caloic transfer rate advantages of higher mutually.
Yet the mixing time of existing airlift reactor is generally greater than the mixing time of bubble tower, and is not ideal enough especially for the highly viscous liquid effect, mainly is that the same mixture contact is relatively poor; By contrast, the aeration-agitation reactor relies on mechanical agitation to help to disperse gas, can adapt to the high viscosity liquid operation.In recent years, can effectively address this problem by mechanical stirring being introduced the gas lift reactor, but churned mechanically introducing will be lost the intrinsic advantage of a lot of air lift types again, as churned mechanically introducing improved airlift reactor energy consumption, increased the internal motion parts, many biochemical reaction systems can't be carried out; Waste of energy is inhomogeneous etc.
Have many high consumption solid/liquid/gas reactions in chemical industry and biological fermentation field, though in traditional reactor by supercharging with improve aeration rate and can partly address this problem, but supercharging causes other gas solubilities to increase, as sour gas CO during the fermentation
2The increase of meltage will cause the acute variation of system environment.The simple raising aeration rate that relies on then can cause the increase of flow stream velocity in the airlift reactor and the raising of running cost.
In addition, exist different step of reaction in many chemical reactions or biological fermentation process, each stage is different with the requirement of air flow to mixing.But existing airlift reactor mixes and ventilation is a coupled problem, and the constant then troubled water of the condition of ventilation is constant, and the constant then aeration status of same troubled water is also inevitable constant.Therefore, can't in a covering device, realize reinforcement to each stage of reaction process.
Simultaneously, continuously ferment and successive reaction will greatly reduce facility investment expense and running cost, but to relating to the reaction of liquid-solid two-phase, existing airlift reactor can't be realized liquid-solid separation, therefore also can't implementation procedure carry out continuously.Existing membrane bioreactor mostly is is with the slurry reactor and the film separating system that stir integrated, can realize successive reaction.Proposed a kind of ceramic membrane Reaction Separation system among the ZL 01 1 08189.9, this system contains biochemical reactor and the film pipe separator that is linked to be the recycle system, and system operates under negative pressure, can solve membrane pollution problem effectively by recoil aeration and gas lift aeration.Yet this system only is a kind of gas lift aerating system, the structure of its reactor is not an airlift reactor, its gas lift circulation is only at pipeline, and mixing efficiency in reactor body and mass-transfer efficiency are all lower, and can't satisfy the continuous film aeration and separate continuously and to the requirement of controlling respectively of mixing efficiency and mass-transfer efficiency.
In sum, develop a kind of novel gas lift type membrane reactor chemical industry and fermentation industry are all had major and immediate significance.
Summary of the invention
The purpose of this utility model is: in order to solve the problems referred to above that exist in the airlift reactor, and a kind of high mixing efficiency, high mass transfer efficiency are provided, can the mixing efficiency in each stage of reaction process and mass transfer are optimized and can realize successive reaction at different step of reaction, be used for the outside circulation gas lift type membrane reactor of gas-liquid two-phase or gas-liquid-solid three-phase process.This reactor still can keep higher mixing and mass-transfer efficiency under the condition of high viscosity, high oxygen consumption, and can be optimized mixing efficiency and mass transfer at each stage of reaction, with reach strengthen react effect, particularly this reactor can be used for relating to the successive reaction of liquid-solid two-phase.
The technical solution of the utility model is: developing thought is that thinking integrated according to the flow process in the field of chemical engineering and that reaction is strengthened is carried out.Main technical schemes is as follows: a kind of outside circulation gas lift type membrane reactor, comprise reactor kettle 2, air-lift tube 5 compositions, it is characterized in that mineral membrane element 7 is encapsulated in the air-lift tube 5, mineral membrane plays the radial distribution device of gas or the effect of separator, the top of air-lift tube has valve 8, and the bottom of air-lift tube has valve 6.
On the basis of such scheme, feature of the present utility model is that also air-lift tube quantity is more than 2 or 2, form the multitube outside circulation gas lift type membrane reactor, the multitube outer circulation can realize continuous aeration and continuous isolating function, and the concrete quantity of air-lift tube is according to reaction aeration efficient and separation efficiency and mix the requirement decision; The multitube outside circulation gas lift type membrane reactor of preferred 2 air-lift tubes, reactor kettle 2 is communicated with air- lift tube 5,13, and mineral membrane element 7,12 is encapsulated in respectively in the air- lift tube 5,13, and mineral membrane can be used as the radial distribution device or the separator of gas.Selecting the air-lift tube number is 2, and wherein 1 provides the required gas of reaction, 1 separation as reaction product in addition as aeration tube, can realize aeration and isolatingly carries out continuously.
Wherein above-mentioned mineral membrane element can be that metallic membrane also can be a ceramic membrane; The aperture is 20nm～100 μ m; Mineral membrane element 7 can be identical membrane element with 12, also can be the membrane element of different performance and structure.
Wherein the membrane element of encapsulation is single or many ceramic membranes in the air- lift tube 5,13, by concrete aeration or separation requirement decision; The mineral membrane element is single passage or hyperchannel; Channel shape is circular, fan-shaped, square, star or sexangle.
Feature of the present utility model is that also reactor kettle 2 has form 9, and there is discharge opening 1 the reaction kettle body bottom, and the upper end has venting port 10; Reactor main body 2 comprises expanding reach and contraction section two portions, and its internal diameter ratio is 1.5～5.
Feature of the present utility model is that also air- lift tube 5,13 links to each other with the B of vacuum-lines system with compressed gas source A, be connected with pressurized gas A and open by valve 6,14 controls, be connected with vacuum system B by valve 8,11 controls and open, air-lift tube connects doline flow backwards pipe 4 and axial aeration nozzle 3 for 5,13 times.
Beneficial effect:
1, adopt nozzle to spray bubble along the riser pipe axial direction due in the riser pipe bottom with certain initial velocity, simultaneously, the size of bubble is bigger, so can effectively improve mixing efficiency, owing to need not moving parts, thereby have suitable a lot of system and characteristic of low energy consumption to the moving parts sensitivity.The utility model adopts the tubular membrane aerating system, carry out cross-flow (being cross flow) aeration along the direction of liquid-flow, because membrane pore size is less than 100 μ m, thereby under microvesicle or still condition, make this reactor obtain higher gas-liquid mass transfer efficient, the coupled cross flow aerating system by these two kinds of aeration forms promptly has higher mixing efficiency also can satisfy the requirement of high gas-liquid mass transfer efficient.Simultaneously, can pass through axial aeration and the radially adjusting of aeration rate are changed mixing efficiency and mass-transfer efficiency, can realize reinforcement reaction process in the different steps of same reaction.
2, the utility model can realize relating to the continuous operation of liquid-solid two-phase reaction by the membrane sepn parts are coupling in this reactor, and the reaction efficiency of reactor improves 5～80 times.
3, the utility model is by being coupling in membrane sepn, film aerating system in the same reactor, the continuous aeration that can realize relating to gas-liquid-solid phase reaction with separate continuously, improved the stability of reaction environment and operation.In addition, by selecting the membrane element of different performance, can realize the optimization of separation efficiency and aeration efficient.
4, used membrane element is a mineral membrane in the utility model, thereby can operate under conditions such as high temperature, is fit to the disinfect in situ in some causticity environment of chemical field and the biochemical system.This reactor also has the flow rule of external loop type airlift reactor, and resistance is little, has the dead angle hardly, good heat-transfer, and easily so the degassing is the characteristics that have.Simultaneously, show by experiment, improve membrane flux because the bubble that axial nozzle produces when particularly forming slug flow in liquid, can effectively reduce the pollution condition of separating film module.In addition, owing to can increase aeration area or improve separation efficiency by increasing the riser pipe number, so the non-constant width of this reactor scope of application.
Description of drawings
Fig. 1 is the outside circulation gas lift type membrane reactor synoptic diagram.
Fig. 2 is single pass air-lift tube I-I directional profile figure for Fig. 1 encapsulating film element.
Air-lift tube I-I directional profile figure when Fig. 3 is hyperchannel for Fig. 1 encapsulating film element.
Air-lift tube I-I direction structure sectional view when Fig. 4 encapsulates many ceramic membranes for Fig. 1.
Fig. 5 is a multitube outside circulation gas lift type membrane reactor synoptic diagram.
Fig. 6 is a cross flow aerating system synoptic diagram in the air-lift tube.
Fig. 7 is a gas lift inner axial tube aeration membrane sepn consolidation system synoptic diagram.
A compressed gas source among the figure, B are vacuum system, and D is a liquid stream main body, and E is a micro-bubble, and F is an air pocket, and G is a product, and H is catalyzer or thalline; 1 is discharge opening, and 2 is the reactor kettle, and 3 is axial aeration nozzle, and 4 are doline refluence pipe, and 5 and 13 is the outside circulation gas lift pipe, and 6,8,11,14 is valve, and 7 and 12 is the mineral membrane element, and 9 is form, and 10 is venting port.
Embodiment
Below in conjunction with description of drawings embodiment of the present utility model.
Embodiment 1:
Outside circulation gas lift type film provided by the utility model is mainly by reactor kettle 2, the outside circulation gas lift pipe 5 that is connected with reactor, and the doline pipe 4 that flows backwards, axially aeration nozzle 3 is encapsulated in the mineral membrane element 7 in the air-lift tube, as shown in Figure 1.Reactor kettle 2 comprises expanding reach and contraction section two portions, and its internal diameter ratio is 1.5～5 usually, and concrete ratio is adjusted according to actual needs, and the reactor kettle has form 9 in order in the observing response device simultaneously.Outside circulation gas lift pipe 5 links to each other with reaction kettle body discharge opening 1 with pipeline by flange, is connected with pressurized gas and opens by valve 6 control, is connected with vacuum system by valve 8 control unlatchings.Axially aeration head connects the pressurized gas generator.
5 are packaged with mineral membrane element 7 in the outside circulation gas lift pipe provided by the utility model, and the material of mineral membrane can be that metal is also ceramic, thereby can realize disinfect in situ, and the aperture can be selected in 20nm～100um scope.The film pipe of encapsulation can be single pass, as shown in Figure 2, also can be as shown in Figure 3 multichannel.The encapsulation the film pipe can be one shown in Fig. 2,3, also can be many, as shown in Figure 4.Can adopt welding process for stainless steel circulation tube and metallic membrane, directly be welded on the flange, then adopt the standard packaging assembly of ceramic membrane to encapsulate ceramic membrane.
The operating method of outside circulation gas lift type film provided by the utility model is as follows: pressurized gas is pressed into air-lift tube by axial aeration head 3, generation have certain initial velocity than air pocket F, axial impellent and bigger density difference are provided, liquid stream main body D is moved upward along air-lift tube.When realizing aeration performance, valve-off 8, Open valve 6, pressurized gas C radially passes through fenestra, is pressed in the inorganic film tube 7,12 with the form of microvesicle E, forms the cross flow aerating system, as shown in Figure 6.The liquid stream main body that has mixed gas enters the part separation of the expanding reach realization gas-liquid of reactor kettle 2, causes density difference and forms downward fluid, and isolated tail gas is discharged by venting port 10.When realizing separation function, open 8, valve-off 6, by pressing in vacuum take-off and the reactor liquid was pressed fenestra, catalyzer or thalline H are trapped, and product G shifts out through film separating system, and pressurized gas is pressed into air-lift tube by aeration head 3, generation is strengthened the membrane sepn process than air pocket, as shown in Figure 7.
Embodiment 2:
Multitube outside circulation gas lift type film provided by the utility model is mainly by reactor kettle 2, the outside circulation gas lift pipe 5 and 13 that is connected with reactor, and the doline pipe 4 that flows backwards, axially aeration nozzle 3 is encapsulated in the mineral membrane element 7,12 in the air-lift tube, as shown in Figure 5.Outside circulation gas lift pipe 5,13 links to each other with reaction kettle body discharge opening 1 with pipeline by flange, is connected with pressurized gas and opens by valve 6,14 control, is connected with vacuum system by valve 8,11 control unlatchings.Axially aeration head connects the pressurized gas generator.
5,13 are packaged with mineral membrane element 7,12 in the outside circulation gas lift pipe provided by the utility model, and mineral membrane element 7,12 can be the same film element, also can select the membrane element of different performance according to the realization of its concrete function.
The operating method of multitube outside circulation gas lift type film provided by the utility model is as follows: pressurized gas is pressed into air-lift tube by axial aeration head 3, generation have certain initial velocity than air pocket F, axial impellent and bigger density difference are provided, liquid stream main body D is moved upward along air-lift tube.When realizing aeration performance, valve-off 8,11, Open valve 6,14, pressurized gas C radially passes through fenestra, is pressed in the inorganic film tube 7,12 with the form of microvesicle E, forms the cross flow aerating system, as shown in Figure 6.The liquid stream main body that has mixed gas enters the part separation of the expanding reach realization gas-liquid of reactor kettle 2, causes density difference and forms downward fluid, and isolated tail gas is discharged by venting port 10.When realizing separation function, open 8,11, valve-off 6,14, by pressing in vacuum take-off and the reactor liquid was pressed fenestra, catalyzer or thalline H are trapped, and product G shifts out through film separating system, and pressurized gas is pressed into air-lift tube by aeration head 3, generation is strengthened the membrane sepn process than air pocket, as shown in Figure 7.Different with reactor among Fig. 1, Open valve 6,11, the aeration of valve-off 8,14 realization response simultaneously device with separates continous-stable and operates.
The novel airlift reactor that the utility model is related can be used for relating to gentle liquid-solid chemistry of gas-liquid and biological process, prepares fields such as organic acid, fermentation legal system ethanol, albumen are cultivated, methyl alcohol is synthetic as wastewater treatment, fermentation method.
Claims (10)
1. outside circulation gas lift type membrane reactor, form by reactor kettle (2), air-lift tube (5), it is characterized in that mineral membrane element (7) is encapsulated in the air-lift tube (5), mineral membrane plays the radial distribution device of gas or the effect of separator, the top of air-lift tube has valve (8), and the bottom of air-lift tube has valve (6).
2. reactor according to claim 1 is characterized in that described air-lift tube is more than 2 or 2.
3. reactor according to claim 1 and 2, it is characterized in that described air-lift tube is 2, reactor kettle (2) is communicated with air-lift tube (5), (13), promptly constitute the multitube outside circulation gas lift type membrane reactor, mineral membrane element (7), (12) are encapsulated in respectively in air-lift tube (5), (13).
4. reactor according to claim 1 is characterized in that the mineral membrane element is metallic membrane or ceramic membrane; The aperture is 20nm～100 μ m.
5. reactor according to claim 3 is characterized in that mineral membrane element (7) and (12) are identical membrane element or are the membrane element of different performance and structure.
6. reactor according to claim 1 is characterized in that can encapsulating in the every air-lift tube single or many ceramic membranes.
7. reactor according to claim 1 is characterized in that the mineral membrane element is single passage or hyperchannel; Channel shape is circular, fan-shaped, square, star or sexangle.
8. reactor according to claim 1 is characterized in that reactor kettle (2) has form (9), and there is discharge opening (1) the reaction kettle body bottom, and the upper end has venting port (10).
9. reactor according to claim 3, it is characterized in that air-lift tube (5), (13) link to each other with vacuum-lines system (B) with compressed gas source (A), be connected by valve (6), (14) control unlatching with compressed gas source A, be connected by valve (8), (11) control with vacuum system B and open; Connect doline refluence pipe (4) and axial aeration nozzle (3) under air-lift tube (5), (13).
10. reactor according to claim 1 is characterized in that reactor main body (2) comprises expanding reach and contraction section two portions, and its internal diameter ratio is 1.5～5.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2005200751399U CN2841645Y (en) | 2005-09-02 | 2005-09-02 | External circulation airlift membrane reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2005200751399U CN2841645Y (en) | 2005-09-02 | 2005-09-02 | External circulation airlift membrane reactor |
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| Publication Number | Publication Date |
|---|---|
| CN2841645Y true CN2841645Y (en) | 2006-11-29 |
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| Application Number | Title | Priority Date | Filing Date |
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| CNU2005200751399U Expired - Fee Related CN2841645Y (en) | 2005-09-02 | 2005-09-02 | External circulation airlift membrane reactor |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103045293A (en) * | 2012-12-13 | 2013-04-17 | 中国科学院过程工程研究所 | Airlift biological desulfurization reactor and desulfurization method |
| CN105779273A (en) * | 2016-04-26 | 2016-07-20 | 淮南师范学院 | Horizontal internal and external double-circulation airlift bioreactor |
| CN112958012A (en) * | 2021-03-19 | 2021-06-15 | 深圳市一正科技有限公司 | Dynamic mixing continuous flow reactor and multistage reaction device |
-
2005
- 2005-09-02 CN CNU2005200751399U patent/CN2841645Y/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103045293A (en) * | 2012-12-13 | 2013-04-17 | 中国科学院过程工程研究所 | Airlift biological desulfurization reactor and desulfurization method |
| CN105779273A (en) * | 2016-04-26 | 2016-07-20 | 淮南师范学院 | Horizontal internal and external double-circulation airlift bioreactor |
| CN112958012A (en) * | 2021-03-19 | 2021-06-15 | 深圳市一正科技有限公司 | Dynamic mixing continuous flow reactor and multistage reaction device |
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