CN105505749A - Air-liquid dual injection type airlift loop reactor - Google Patents
Air-liquid dual injection type airlift loop reactor Download PDFInfo
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- CN105505749A CN105505749A CN201610124569.8A CN201610124569A CN105505749A CN 105505749 A CN105505749 A CN 105505749A CN 201610124569 A CN201610124569 A CN 201610124569A CN 105505749 A CN105505749 A CN 105505749A
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- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M27/00—Means for mixing, agitating or circulating fluids in the vessel
- C12M27/18—Flow directing inserts
- C12M27/24—Draft tube
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- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M29/00—Means for introduction, extraction or recirculation of materials, e.g. pumps
- C12M29/06—Nozzles; Sprayers; Spargers; Diffusers
- C12M29/08—Air lift
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- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M29/00—Means for introduction, extraction or recirculation of materials, e.g. pumps
- C12M29/18—External loop; Means for reintroduction of fermented biomass or liquid percolate
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Abstract
The invention relates to an air-liquid dual injection type airlift loop reactor comprising a fermentation tank. The air-liquid dual injection type airlift loop reactor is characterized in that guide cylinders are arranged in the fermentation tank, a liquid ascending area is arranged inside each guide cylinder, a liquid descending area is arranged among the guide cylinders and the fermentation tank, an annular distribution pipe is mounted on the lower portion of the liquid ascending area and provided with a plurality of spray holes, one or more static spiral cutting devices are mounted at the bottom of the fermentation tank, and each static spiral cutting device is provided with an air-liquid mixture outlet, a fermentation liquid input inlet and a compressed air input inlet, wherein the compressed air input inlet is connected with an air source, the air-liquid mixture outlet is connected with the distribution pipe, and the fermentation liquid input inlet is connected with a circular liquid outlet in the bottom of the fermentation tank through a pipeline. The air-liquid dual injection type airlift loop reactor has the advantages that difficulties in mixed air-liquid delivery and air-liquid coupling of an airlift biological fermentation system are overcome, biological treatment capability of the airlift loop reactor can be given to full play maximally, treatment efficiency is improved and energy consumption is reduced.
Description
Technical field
The present invention relates to a kind of gas-liquid double jet type Airlift circulating reactor, especially a kind of gas-liquid double jet type Airlift circulating reactor based on the micro-nano cutting refinement technology of gas-liquid.
Background technology
Airlift circulating reactor (airlifeloopreactor, be called for short ALR), be a kind of using source of the gas as power, make liquid mixing and the reactor circulated.It is current most widely used biologic reaction equipment.Its principle of work is that sterile air is sprayed in fermented liquid by nozzle or spray orifice, air filled cavity is made to split by the turbulent flow of gas-liquid mixture in small, broken bits, gas-liquid mixture density simultaneously owing to being formed reduces therefore moves upward, the fermented liquid that gas holdup is little then sinks, formation circulates, and realizes mixing and dissolved oxygen mass transfer.This kind of reactor has the advantages such as structure is simple, energy consumption is low, shear-stress is little, mix.Airlift circulating reactor is all quite favourable for the mixing between reactant and mass transfer.Airlift circulating reactor is the novel reactor improved by bubbling reactor, it combines the performance of bubbling bed and stirring tank, compared with bubbling bed reactor, loop reactor has the feature of liquid directed flow, under lower superficial gas velocity, namely can realize the suspension completely of solid particulate, and be applied to numerous areas such as F-T synthesis, one-step synthesis method methyl alcohol and dme, gasoline desulfur, heavy oil hydrogenation, biological useless fermentation liquor treatment and fermentation engineering etc. at present.
The ALR of industrial application has internal-circulation type and outer circulation type two type, and the reactor of which kind of type is all made up of 4 main parts: at the bottom of ascent stage, downcomer, device and gas-liquid separator.The fluid flow characteristics at each position is each variant, and matrix transmission, product are formed, thermal exchange situation is also different throughout.This two classes reactor is compared, outer circulation airlift reactor can fall liquid zone mounting heat exchanger to strengthen heat transfer, be convenient to measurement and the control of ascent stage and downcomer, also a throttling valve can be installed between ascent stage and downcomer, to control air inlet rate and liquid circulation velocity.Internal circulation gas-lift type reactor then structure comparison is compact, guide shell can make multistage to strengthen local and totally to circulate, also can mounted sieve in guide shell, gas distribution is improved, and suitably can suppresses liquid circulation velocity.
Compared with other reactors, ALR has that structure is simple, shearing force is low, air feed efficiency is high, effective interface contact area is comparatively large, splendid, each phase of fluid effect has the clear and definite residence time and Mass and heat transfer speed advantages of higher.But being found by research and practical application, also there are following shortcomings in it: initialize investment is larger; Need very large throughput of air; Alternate mixing contact is poor; When the organism circulated and operational condition change, substrate, nutrition and oxygen level can not be consistent; When there is foam, the poor effect of gas-liquid separation; Namely mixing and gas-liquid coupled problem, be also difficult to improve under the condition not changing ventilation.
Summary of the invention
The object of the invention is to overcome the deficiencies in the prior art, a kind of gas-liquid double jet type Airlift circulating reactor is provided, overcome air lift type Biofermentation system gas-liquid delivery and send the difficult point with gas-liquid coupling, play the biological treatment capabilities of Airlift circulating reactor to greatest extent, improve processing efficiency, reduce energy consumption.
According to technical scheme provided by the invention, a kind of gas-liquid double jet type Airlift circulating reactor, comprise fermentor tank, feature is: in described fermentor tank, arrange guide shell, the inside of guide shell is liquid rising area, be liquid decline district between guide shell and fermentor tank, install annular distribution pipe in the bottom of liquid rising area, distribution pipe is provided with multiple spray orifice; One or more static ribbon cutting units are installed in the bottom of described fermentor tank, static ribbon cutting unit have gas-liquid mixture outlet, fermented liquid input aperture and pressurized air input aperture, pressurized air input aperture is connected with air source of the gas, gas-liquid mixture outlet is connected with distribution pipe, and fermented liquid input aperture is connected with the fluid circulation port of fermenter base by pipeline.
Further, fermentation liquid pump is set between the fermented liquid input aperture and the fluid circulation port of fermentor tank of described static ribbon cutting unit.
Further, described static ribbon cutting unit comprises cutting pipe, and cutting tube hub arranges mandrel, and the liquid feeding end of mandrel arranges drain cone; Described mandrel is arranged some successively spiral superposition cutting blade; Inflating valve is connected at the liquid feeding end of described cutting pipe, axial centre aerator is installed in inflating valve, axial centre aerator comprises the base be arranged on inflating valve, in base, airway is set, the outer end of airway connects inlet pipe, in the inner of airway, throttle seat is installed, in throttle seat, throttling valve core is set, throttle seat is arranged and adds pore.
Further, described cutting blade has three or more blade.
Further, described cutting blade forms along the superposition of mandrel length direction successively spiral three or many spirals being arranged by mandrel length direction, and the blade of adjacent two cutting blades to stagger certain angle according to helix equation, forms stepped cutting cutting edge in spiral side.
Further, the volution that the cutting blade of described spiral superposition is formed adopts varying pitch, and the pitch of liquid feeding end is greater than the pitch of outlet end, and pitch is reduced to outlet end gradually by liquid feeding end.
Further, the thickness of described cutting blade is 0.08 ~ 5mm.
Further, add pore and inflating valve described in, cut the axis coaxle of pipe.
Further, between described inflating valve and cutting pipe, static mixer is installed.
The present invention has the following advantages:
(1) air macromolecular mass is cut into the subset material of micro-nano magnitude by the present invention by the static ribbon cutting unit of actuating unit without spin, almost be dissolved at normal temperatures and pressures in fermented liquid, dissolved oxygen content is high, and dissolved oxygen rate increases 4-5 times, good stability than conventional gas lift formula fermentation method; Static ribbon cutting unit is unpowered rotating mechanism, equipment cost is low, easy care, can realize large-scale commercial production and application.
(2) static ribbon cutting unit of the present invention can realize gas-liquid micro-nanoization cutting refinement, and gas-liquid is all subject to shearing force in cutting chamber XYZ tri-directions; Border, flow field is the stepped cutting edge of cut-off blade spiralization, and under the effect of certain field of flow and centrifugal force, gas-liquid is subject to the cutting force of stepped cutting edge, can realize the cutting of infinitely small yardstick in theory.
(3) the present invention is the spiral cutter device of air by static discretize, cutting is fast and efficiently refined as the small bubbles of micro-nano magnitude, greatly improve the dissolved efficiency of oxygen, in fermented liquid, dissolved oxygen amount can reach the 4-5 of traditional zymotic tank gas entrainment method doubly, and dissolved oxygen stable is good.
(4) aerator of the present invention adopts inflating valve, the air outlet of particular design, Hydrodynamics Theory according to laminar fluid Circular Cylinder body is analyzed known, add the flow velocity of pore near zone fermented liquid close to 0, oxygen can be emitted in fermented liquid smoothly, realize helical cutters four the cutting even aerating in chamber, this gas entrainment method efficiency is high, and cutting refinement is even.
(5) instant invention overcomes conventional gas lift formula Biofermentation system gas-liquid delivery and send the difficult point with gas-liquid coupling, Ventilation Rate and the gas-liquid blending transportation of 1-10VVM can be realized.
Accompanying drawing explanation
Fig. 1 is the structural representation of gas-liquid double jet type Airlift circulating reactor of the present invention.
Fig. 2 is the structural representation of described static ribbon cutting unit.
Fig. 3 is the schematic diagram of described cutting blade.
Fig. 4 is the working state schematic representation of described static ribbon cutting unit.
Embodiment
Below in conjunction with concrete accompanying drawing, the invention will be further described.
As shown in Figure 1 to 4: described gas-liquid double jet type Airlift circulating reactor comprises fermentor tank 1, guide shell 2, fermentation liquid pump 3, distribution pipe 4, static ribbon cutting unit 5, spray orifice 6, inflating valve 3-1, base 3-2, airway 3-3, sealing-ring 3-4, sealing block 3-5, throttle seat 3-6, throttling valve core 3-7, adds pore 3-8, flange 5-1, cutting pipe 5-2, mandrel 5-3, drain cone 5-4, cutting blade 5-5, briquetting 5-6, set nut 5-7, blade 5-8 etc.
As shown in Figure 1, gas-liquid double jet type Airlift circulating reactor of the present invention, comprises fermentor tank 1, and the material that fermentor tank 1 adopts is SUS316L, and nominal volume selects 500L; In described fermentor tank 1, arrange guide shell 2, guide shell 2 adopts existing commercially available molybdenum guide shell; The inside of described guide shell 2 is liquid rising area, and be liquid decline district between guide shell 2 and fermentor tank 1, install annular distribution pipe 4 in the bottom of liquid rising area, distribution pipe 4 is provided with multiple spray orifice 6.
In the bottom of described fermentor tank 1, one or more static ribbon cutting units 5 are installed, static ribbon cutting unit 5 have gas-liquid mixture outlet, fermented liquid input aperture and pressurized air input aperture, pressurized air input aperture is connected with air source of the gas, gas-liquid mixture outlet is connected with distribution pipe 4, and fermented liquid input aperture is connected with the fluid circulation port bottom fermentor tank 1 by pipeline; Between the fermented liquid input aperture and the fluid circulation port of fermentor tank 1 of described static ribbon cutting unit 5, arrange fermentation liquid pump 3, fermentation liquid pump 3 adopts commercially available sanitation-grade stainless steel vacuum primingpump.
As shown in Figure 2, described static ribbon cutting unit 5 comprises cutting pipe 5-2, and cutting pipe 5-2 center arranges mandrel 5-3, and the liquid feeding end of mandrel 5-3 arranges drain cone 5-4, the effect of drain cone 5-4 is to make gas-liquid mixed stream equal, can uniformly across cutting pipe 5-2 after diffusion; Described mandrel 5-3 is arranged some successively spiral superposition cutting blade 5-5, the centre hole of cutting blade 5-5 and mandrel 5-3 running fit, cutting blade 5-5 is fixed on mandrel 5-3 by briquetting 5-6 and set nut 5-7; Described cutting blade 5-5 having in three or more blade 5-8(Fig. 4 is 4 blade 5-8), cutting blade 5-5 forms along the superposition of mandrel 5-3 length direction successively spiral three or many spirals being arranged by mandrel 5-3 length direction, and the blade 5-8 of adjacent two cutting blade 5-5 to stagger certain angle according to helix equation, forms stepped cutting cutting edge in spiral side.Described volution adopts varying pitch, and the pitch of liquid feeding end is greater than the pitch of outlet end, and pitch is reduced to outlet end gradually by liquid feeding end.The thickness of described cutting blade 5-5 is 0.08 ~ 5mm.
As shown in Figure 2, connect inflating valve 3-1 at the liquid feeding end of described cutting pipe 5-2, generally between inflating valve 3-1 and cutting pipe 5-2, static mixer (not shown) is also installed; In described inflating valve 3-1, axial centre aerator is installed, axial centre aerator comprises the base 3-2 be arranged on inflating valve 3-1, airway 3-3 is set in base 3-2, arrange sealing-ring 3-4 and sealing block 3-5 between airway 3-3 and base 3-2, sealing block 3-5 is by nut and screw fastening; The outer end of described airway 3-3 connects inlet pipe, inlet pipe is connected with source of the gas, in the inner of airway 3-3, throttle seat 3-6 is installed, in throttle seat 3-6, throttling valve core 3-7 is set, on throttle seat 3-6, setting adds pore 3-8, add pore 3-8 and inflating valve 3-1, cut the axis coaxle of pipe 5-2, right alignment is less than 0.1mm, can ensure that gas is emitted in water smoothly.
Principle of work of the present invention: gas-liquid double jet type Airlift circulating reactor of the present invention, adopt micro-nano cutting refinement technology, biphase gas and liquid flow is cut refinement by static ribbon cutting unit 5 by gas-liquid two-phase, air macromolecular mass is cut into the subset material of micro-nano magnitude, be dissolved in fermented liquid by less pressure and certain field of flow effect, almost realize highly effective oxygen dissolving at normal temperatures and pressures, dissolved oxygen rate increases 4-5 doubly than conventional gas lift formula fermentation gas entrainment method.Fermented liquid oxygen level is high, and containing oxidation stability, the transformation period reaches 20 days.Preparation cost is low, device simple, easy to maintenance.
Described static ribbon cutting unit 5 rotates superposition by several thousand cutting blades according to varying pitch and forms the stepped spiral camber of discretize.Utilize the pressure of self and the flow velocity of gas-liquid, fermented liquid and air draught cross cutting chamber, due to variable-pitch auger structure special in cutting chamber, form the existence of internal fluid x, y, z three-dimensional velocity gradient, therefore internal fluid is all subject to shearing force on x, y, z three directions; And fluid in boundary surface with discretize, cutting blade that thickness is only 5mm tires out folded stepped helical cut edge contacts, suppose that fluid is motionless, be equivalent to the blade of unlimited multi-blade at cutting fluid, the subset material with joint efforts gas-liquid being slit into micro-nano magnitude of two effects, the continuous pressurized expansion of the bubble of nanometer scale self, finally explosion is dissolved in fermented liquid, adds liquid dissolving oxygen amount in fermentor tank.
The axial line right alignment adding pore 3-8 and inflating valve 3-1, cut pipe 5-2 of described axial centre aerator is less than 0.1mm, Hydrodynamics Theory according to laminar fluid Circular Cylinder body is analyzed known, add the flow velocity of pore 3-8 near zone liquid close to 0, air can be emitted in fermented liquid smoothly, realize the cutting pipe cutting even aerating in chamber, this gas entrainment method efficiency is high, and cutting refinement is even.Add the effect of pore near zone due to fluid, can underbalance effect be formed, under air pressure is slightly less than hydraulics, also can realizes aerating smoothly, reduce equipment energy consumption.Test determination dissolved oxygen rate is 4-5 times of the direct aeration of conventional gas lift formula fermentor tank pressurized air.
Working process of the present invention: during the work of gas-liquid double jet type Airlift circulating reactor, forced air G enters static variable-pitch propeller cutting unit 5 by the pore 3-8 injection that adds of inflating valve 3-1, fermented liquid pumps into static variable-pitch propeller cutting unit 5 by fermentation liquid pump 3 simultaneously, utilize fermented liquid and compressed-air actuated self pressure and flow velocity, fermented liquid and air flow through cutting chamber, realize cutting and the blending transportation of the micro-nano magnitude of gas-liquid, it is inner that gas-liquid mixture enters guide shell 2 by the nozzle of ring-like distribution pipe.The continuous pressurized expansion of the bubble of nanometer scale self, finally explosion is dissolved in fermented liquid, improves dissolved oxygen rate, and dissolved oxygen rate is 4-5 times of traditional gas entrainment method.The specific surface area of micro-nano bubble sharply increases, and heat transfer in guide shell between liquid phase, mass transfer and biochemical reaction process are sharply strengthened, both close contacts thus fully react.Because the gas-liquid mixture density formed in guide shell can reduce, add that air is by the kinetic energy after compressing, and therefore can make the liquid flows upwards in guide shell; After arriving reactor top liquid level, gas G in part gas-liquid mixture is discharged to the upper space of reactor, because the liquid of discharge section gas is flowed outside guide shell by guide shell top, liquid outside guide shell reduces because becoming gas holdup after Exhaust Gas, density increases, so liquid can drop to reactor bottom under gravity.At reactor bottom because the liquid velocity in guide shell is very large, liquid little for gas holdup can be sucked guide shell inside and again enter upcast participation reaction, thus formation one circulates, and realizes mixing and mass transfer.
Static discretize variable-pitch propeller cutting unit is the core component of this device, is the composition such as the variable-pitch propeller cut-off blade of 0.08-5mm and stationary installation primarily of thickness.These parts can realize the cutting refinement of gas-liquid micro-nanoization and blending transportation.Static variable-pitch propeller cutter chamber have employed special varying pitch design, is namely the fine pitch of fluid outlet by the coarse pitch transition of fluid intake, and 4 helical cut chambeies are that 0.08-5mm cut-off blade to superpose according to the blocks of spiral of helix equation and formed by thickness.Due to variable-pitch auger mechanism, gas-liquid is all subject to shearing force in space X YZ tri-directions; Border, flow field is the stepped cutting edge of cut-off blade spiralization, under the effect of certain field of flow and centrifugal force.Bubble and fermented liquid are subject to the cutting force of stepped cutting edge, can realize the cutting of infinitely small yardstick in theory.
Static variable-pitch propeller cutting unit working state schematic representation as shown in Figure 4.7 is fermented liquid input aperture, and 8 is pressurized air input aperture, and pressurized air input aperture 8 is connected with air source of the gas.9 is gas-liquid mixture outlet, is connected with the ring-like distribution pipe of fermentor tank.Utilize fermented liquid and compressed-air actuated self pressure and flow velocity, fermented liquid and air flow through cutting chamber, realize cutting and the mixing of the micro-nano magnitude of gas-liquid, the continuous pressurized expansion of the air filled cavity of nanometer scale self, finally explosion is dissolved in fermented liquid, and dissolved oxygen rate is 4-5 times of conventional gas lift formula fermentor tank gas entrainment method.In guide shell, the contact gear ratio surface-area of fermented liquid and micro-nano bubble sharply increases, and enhances both heat transfers, mass transfer and biochemical reaction process, reaches the object of energy-saving and emission-reduction.
Major advantage of the present invention is as follows:
(1) static for gas-liquid micro-nanoization variable-pitch propeller cutting unit is arranged on airlift fermentor air nozzle front end, under same gas degree of refinement, greatly can reduce spraying pressure and the flow velocity of pressurized gas, (conventional gas lift formula fermentation container blast injection gas speed will reach 250 ~ more than 300m/s to reach energy-conservation object, turbulent flow just by liquid-vapor mixture makes air bubble segmentation in small, broken bits, forms certain contact area).Meanwhile, the continuous pressurized expansion of the air filled cavity of micro-nano magnitude self, finally explosion is dissolved in fermented liquid, defines highly effective oxygen dissolving, and dissolved oxygen rate increases 4-5 doubly than conventional gas lift formula fermentation gas entrainment method.In guide shell, the contact gear ratio surface-area of fermented liquid and micro-nano bubble sharply increases, and enhances both heat transfers, mass transfer and biochemical reaction process, accelerates biological fermentation speed, improves fermentation efficiency.
(2) refinement gas-liquid consumption of power is hardly cut, realize fermented liquid highly effective oxygen dissolving at normal temperatures and pressures, dissolved oxygen rate improves 4-5 doubly, and its Air Bubble Size produced is micro-nano magnitude, and the microbubble that this mode produces is formed by physics mode cutting, the dissolved oxygen produced is highly stable, dissolved oxygen rate of fall-off is in a liquid decay 50% in 20 days, for aerobic fermentation reaction provides stable oxygen source, can not produce air pocket and form foam, fermenting process is stablized, improves production capacity.
(3) the present invention forms a kind of novel biological treatment flow process based on gas-liquid micro-nanoization cutting refinement technology and gas-liquid double jet type Airlift circulating reaction technology, formed a kind of fine molecular, the new bio process treatment process of efficient, energy-saving and emission-reduction and method.Oxygen macromolecular mass in air can refine to nanometer scale, and not easily discharge from fermented liquid, the direct aeration high energy consumption of conventional gas lift formula fermentation technique air, inefficient defect are got rid of, improve microorganism to organic decomposition rate, observable index conventional gas lift formula bioreaction technology reduces 25-35%.
(4) cutting of industry high-concentration macromolecular mass harmful organic substance can be refined to micro-nano magnitude by the gas-liquid double jet type Airlift circulating reactor based on gas-liquid micro-nanoization cutting refinement dissolved oxygen technology, biological area is large, intimate mixing is good, mass transfer velocity is high, the Decomposition of microorganism can be given full play to, harmful organic substance is fully decomposed.
Claims (9)
1. a gas-liquid double jet type Airlift circulating reactor, comprise fermentor tank (1), it is characterized in that: guide shell (2) is set in described fermentor tank (1), the inside of guide shell (2) is liquid rising area, it is liquid decline district between guide shell (2) and fermentor tank (1), install annular distribution pipe (4) in the bottom of liquid rising area, distribution pipe (4) is provided with multiple spray orifice (6); One or more static ribbon cutting units (5) are installed in the bottom of described fermentor tank (1), static ribbon cutting unit (5) have gas-liquid mixture outlet, fermented liquid input aperture and pressurized air input aperture, pressurized air input aperture is connected with air source of the gas, gas-liquid mixture outlet is connected with distribution pipe (4), and fermented liquid input aperture is connected by the fluid circulation port of pipeline with fermentor tank (1) bottom.
2. gas-liquid double jet type Airlift circulating reactor as claimed in claim 1, is characterized in that: between the fermented liquid input aperture and the fluid circulation port of fermentor tank (1) of described static ribbon cutting unit (5), arrange fermentation liquid pump (3).
3. gas-liquid double jet type Airlift circulating reactor as claimed in claim 1, it is characterized in that: described static ribbon cutting unit (5) comprises cutting pipe (5-2), cutting pipe (5-2) center arranges mandrel (5-3), and the liquid feeding end of mandrel (5-3) arranges drain cone (5-4); Described mandrel (5-3) is arranged some successively spiral superposition cutting blade (5-5); Inflating valve (3-1) is connected at the liquid feeding end of described cutting pipe (5-2), in inflating valve (3-1), axial centre aerator is installed, axial centre aerator comprises the base (3-2) be arranged on inflating valve (3-1), airway (3-3) is set in base (3-2), the outer end of airway (3-3) connects inlet pipe, in the inner of airway (3-3), throttle seat (3-6) is installed, arrange throttling valve core (3-7) in throttle seat (3-6), the upper setting of throttle seat (3-6) adds pore (3-8).
4. gas-liquid double jet type Airlift circulating reactor as claimed in claim 3, is characterized in that: described cutting blade (5-5) has three or more blade (5-8).
5. gas-liquid double jet type Airlift circulating reactor as claimed in claim 3, it is characterized in that: described cutting blade (5-5) forms along the superposition of mandrel (5-3) length direction successively spiral three or many spirals being arranged by mandrel (5-3) length direction, and the blade (5-8) of adjacent two cutting blades (5-5) to stagger certain angle according to helix equation, forms stepped cutting cutting edge in spiral side.
6. gas-liquid double jet type Airlift circulating reactor as claimed in claim 3, it is characterized in that: the volution that the cutting blade (5-5) of described spiral superposition is formed adopts varying pitch, the pitch of liquid feeding end is greater than the pitch of outlet end, and pitch is reduced to outlet end gradually by liquid feeding end.
7. gas-liquid double jet type Airlift circulating reactor as claimed in claim 3, is characterized in that: the thickness of described cutting blade (5-5) is 0.08 ~ 5mm.
8. gas-liquid double jet type Airlift circulating reactor as claimed in claim 3, is characterized in that: described in add pore (3-8) with inflating valve (3-1), cut the axis coaxle of managing (5-2).
9. gas-liquid double jet type Airlift circulating reactor as claimed in claim 3, is characterized in that: between described inflating valve (3-1) and cutting pipe (5-2), be provided with static mixer.
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN107974395A (en) * | 2016-10-21 | 2018-05-01 | 北京伊克希德化工技术有限公司 | A kind of gas-lifting type aerobic fermentation tower |
| WO2018076414A1 (en) * | 2016-10-28 | 2018-05-03 | 江南大学 | Airlift reactor with helical porous sieve plate |
| CN112619566A (en) * | 2021-01-19 | 2021-04-09 | 中国科学院山西煤炭化学研究所 | Multistage jet loop reactor for preparing ethylene by oxidative coupling of methane |
| CN112808181A (en) * | 2021-01-19 | 2021-05-18 | 中国科学院山西煤炭化学研究所 | Jet loop reactor for preparing ethylene by oxidative coupling of methane |
| CN113302274A (en) * | 2019-01-25 | 2021-08-24 | 联合生物有限公司 | Improved circulation fermenter |
| CN113754478A (en) * | 2021-08-27 | 2021-12-07 | 周晗璐 | Aeration type solid-liquid state beach organic fertilizer, preparation method and fermentation device |
| CN114085753A (en) * | 2021-11-22 | 2022-02-25 | 石家庄吉瑞节能技术有限公司 | Forced circulation flow energy-saving fermentation tank |
| CN114195252A (en) * | 2021-11-26 | 2022-03-18 | 大唐东北电力试验研究院有限公司 | Air-lift reactor for treating and refining soybean oil wastewater by using fermentation type hyphomycete |
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| CN107974395A (en) * | 2016-10-21 | 2018-05-01 | 北京伊克希德化工技术有限公司 | A kind of gas-lifting type aerobic fermentation tower |
| WO2018076414A1 (en) * | 2016-10-28 | 2018-05-03 | 江南大学 | Airlift reactor with helical porous sieve plate |
| CN113302274A (en) * | 2019-01-25 | 2021-08-24 | 联合生物有限公司 | Improved circulation fermenter |
| CN112619566A (en) * | 2021-01-19 | 2021-04-09 | 中国科学院山西煤炭化学研究所 | Multistage jet loop reactor for preparing ethylene by oxidative coupling of methane |
| CN112808181A (en) * | 2021-01-19 | 2021-05-18 | 中国科学院山西煤炭化学研究所 | Jet loop reactor for preparing ethylene by oxidative coupling of methane |
| CN112619566B (en) * | 2021-01-19 | 2022-04-12 | 山西潞安化工有限公司 | Multistage jet loop reactor for preparing ethylene by oxidative coupling of methane |
| CN113754478A (en) * | 2021-08-27 | 2021-12-07 | 周晗璐 | Aeration type solid-liquid state beach organic fertilizer, preparation method and fermentation device |
| CN114085753A (en) * | 2021-11-22 | 2022-02-25 | 石家庄吉瑞节能技术有限公司 | Forced circulation flow energy-saving fermentation tank |
| CN114195252A (en) * | 2021-11-26 | 2022-03-18 | 大唐东北电力试验研究院有限公司 | Air-lift reactor for treating and refining soybean oil wastewater by using fermentation type hyphomycete |
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