CN103146564A - Coaxial different-speed combined oar reactor and industrial application thereof - Google Patents
Coaxial different-speed combined oar reactor and industrial application thereof Download PDFInfo
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Abstract
The invention relates to a coaxial different-speed combined oar reactor and industrial application of the coaxial different-speed combined oar reactor. The coaxial different-speed combined oar reactor comprises a cylindrical vertical container and a stirring device which is axially installed in the cylindrical vertical container. The coaxial different-speed combined oar reactor is characterized in that the stirring device is a combined oar which comprises a spiral band oar stirring oar, a lower layer stirring oar and a bottom stirring oar, wherein the spiral band oar circles on the periphery of a stirring shaft which is arranged in the center of the coaxial different-speed combined oar reactor from top to bottom, the lower layer stirring oar is arranged close to the lower portion of the coaxial different-speed combined oar reactor, and the bottom stirring oar is arranged at the bottom of the coaxial different-speed combined oar reactor. According to the coaxial different-speed combined oar reactor, combination of three types of blades is adopted to provide two types of action including shear and circulation on materials. Under combined action of the two types of flow including the shear and the circulation, the coaxial different-speed combined oar reactor and the industrial application of the coaxial different-speed combined oar reactor has the advantages of enabling the materials which are added into the coaxial different-speed combined oar reactor to be rapidly mixed, enabling distribution of energy consumption in a stirring groove to be even, enabling energy to be effectively used, being capable of solving the problem that materials close to a wall surface stick to the wall surface, strengthening heat transmission, promoting particles to evenly suspend, being simple in structure, facilitating adjustment of structural parameters and operating parameters, and being convenient to machine, manufacture and install.
Description
[technical field]
The present invention relates to the mechanical stirring technical field, specifically, is a kind of coaxial friction speed combination oar reactor and industrial application thereof.
[background technology]
Developing rapidly of modern industry sharply increases the demand of the energy, and the energy major part that world consumes is from fossil resource.Fossil energy not only reserves is limited, and can cause a large amount of NO
x, SO
2Deng obnoxious flavour and CO
2, methane isothermal chamber gaseous emission, become more and more important so the exploitation of environment amenable renewable resources seems.Alcohol fuel more and more receives the concern of various countries as the most promising a kind of renewable energy source.
The now production of alcohol fuel mainly with sugar crops (Brazil) and corn (U.S.) as raw material, its output is subject to the restriction of grain resource, and raw materials cost is up to 40% of total cost, be difficult to satisfy for a long time energy demand, take a long view and must seek abundant and cheap raw material sources, the research of this respect recently mainly concentrates on lignocellulose.Lignocellulosic material takes up an area 50% of ball total biomass according to statistics.Mainly comprise: 1. agricultural wastes, as wheat straw, maize straw, corn cob, soybean residue, bagasse etc.; 2. trade waste is as the fibrous residue in slurrying and paper mill, sawdust etc.; 3. forestry waste; 4. urban waste is as waste paper, wrapping paper etc.The raw material of lignocellulose and waste, its composition is the carbohydrate aggregate, comprises Mierocrystalline cellulose, hemicellulose, dextran and xylogen.Originally these materials use various chemistry usually, and mechanical processes with main release hexose and pentose with enzyme method, thereby but subsequent fermenting is useful product.These processing are variant aspect complicacy and efficient.
Produced the technique of alcohol fuel by Mierocrystalline cellulose, basically can be divided into two classes, the first kind is SHF technique, i.e. the fermentation of cellulosic hydrolysis and liquid glucose is carried out in different reactors; Equations of The Second Kind is SSF technique, i.e. cellulosic hydrolysis and fermentation are carried out in same reactor.SSF has not only simplified production equipment, and because of the cellulose hydrolysis speed in fermentor tank far below glucose fermentation speed, make the concentration of glucose in solutions and cellobiose very low, this has just eliminated them as the restraining effect of hydrolysate to enzymic hydrolysis, the corresponding consumption that reduces enzyme.Low glucose concn has also reduced the chance that miscellaneous bacteria infects in addition.SSF has become up-and-coming biomass-making alcohol technique at present.
Produce ethanol as example take the maize straw simultaneous saccharification and fermentation, analyze its reaction engineering characteristic, roughly can be summarized as following some:
One, investigate the dynamics of enzymatic hydrolysis reaction, its characteristics are as follows, at first enzyme must be adsorbed to cellulose surface (adsorptive capacity meets the Langmuir adsorption isothermal line), this adsorption equilibrium process required time is probably several minutes, and the enzyme that is adsorbed is subsequently to the Mierocrystalline cellulose effect, and it is very fast making the used time initial rate, along with after hydrolysis carries out several minutes, hydrolysis rate significantly descends, and after hydrolysis 24h, hydrolysis rate is less than 2% of initial hydrolysis rate.This shows, for whole hydrolytic process, although its required time very long (having technological process even to reach several days), most important process is at initial several minutes, this just require lytic enzyme, bacterial classification can be in the stalk material short mix and be adsorbed onto cellulose surface.
two, investigate the consumption of enzyme (bacterial classification) and the ratio of the consumption of stalk material, easily find, both amounts differ greatly, in addition, the viscosity of lytic enzyme (bacterial classification) is far below the viscosity of stalk material, for the mixing of comparing the different sticking system that differs greatly, its hybrid technology will be difficult many, this is just to material (maize straw material, lytic enzyme, bacterial classification) feed way is (especially for a large amount of stalk materials, disposablely to add or add in batches, if add in batches, feed time is for how long, what is the amount that at every turn adds again?), feed location, the stirring rake mixed performance is had higher requirement.Similarly, in reactor, the control of pH value has identical problem.
Three, investigate the phase-state change of maize straw material in whole diastatic fermentation process, its process is as follows: in several hours of initial liquefaction, the biomass structure is degraded, and in reactor, material changes dense thick starchiness into gradually by solid-state; Along with deeply carrying out of liquefaction process, the structure completely dissolve of maize straw, material is liquid by solid state transformation; In follow-up saccharification and fermenting process, the viscosity of material continues to reduce, and after reaction finished, in reactor, material was slurry or suspension liquid shape.In addition, in fermenting process, system has CO
2γ-ray emission, this moment, system was the gas-liquid-solid three-phase complex system.This shows, for SSF technique, in same reactor, the viscosity of system has experienced by height and has adhered to low sticking dynamic transition process, and this just requires designed saccharification reactor can have mixed performance preferably in the different viscosity stage.In the reaction later stage, the discharge of the suspension of solid phase, the gas of generation is also the problem that must consider.
Four, frontly address, at first cellulase must be adsorbed onto the cellulose surface reaction that just can be hydrolyzed, and from the mass transfer angle, the granularity of stalk material is less, and the contact area of itself and cellulase is larger, and hydrolysis effect is better.Just in reactor, the stalk raw meal particle size proposes certain requirement to joining for this.
Five, for saccharification and fermentation reaction, need to keep and carry out at a certain temperature, at 45～55 ℃, the optimum temps of fermentation reaction is at 28～33 ℃ for the optimum temps of saccharification react.This will the appropriate design reactor jacket and the heating operation mode of reactor, makes the reactor heat transfer property can satisfy reaction needed.
In order to carry out above-mentioned technique, various equipment have been used in dissimilar biomass, carry out different processing, comprise small-scale process exploitation and some full-scale plants.the kind of some equipment is used, comprise batch stirred tank reactor (Gusakov and Sinitsyn, 1985Enz.Microb.Technol.7:346-352, CN101090962A, CN101160388A), Continuous Flow stirred reactor (US4257818), griding reaction device (Ryu and Lee (1983) Biotechnol.Bioeng.25:53-65) extruding reaction device (US6176176), NREL shrinks bed (shrinking bed) reactor (people such as Lee, 2001, Appl.Biochem.Biotech.91-93:331-340) and the reactor that strengthen to stir of the electromagnetic field inducing (people such as Gusakov, (1996) Appl.Biochem.Biotech.56:141-153).
Above-mentioned reactor, except Chinese patent CN101090962A, other more early stage reactors are applicable to be hydrolyzed respectively and zymotechnique, type of reactor mostly is the hydrolysis process device, its structure focuses on the grinding to cellulose substances more, to increase lytic enzyme and cellulosic contact area, strengthens hydrolysis effect, thereby caused the reactor inner member too complicated, be unfavorable for industrialization.Chinese patent CNl01160388A has announced a kind of equipment of processing biomass, and rotatable baffle plate, grinding medium (comprising free floating at the pill of this reaction vessel interior) that this equipment has the container inside of being connected to reach the injection lance for delivery of the device of processing reagent.This equipment is only applicable to hydrolysis process equally, and device structure is too complicated, is unfavorable for industrialization.Chinese patent CN101090962A combines enzymic hydrolysis and depends on and guarantees that mechanical force (being mainly shearing force and tear edge) is applied to the mixed type of the gravity principle of biomass; select the free-falling mixing machine such as drum mixer, tilting concrete mixer or similar mixing device; its mixing principle is mainly gravity diffusive mixing radially, and axially convection current is less.Simultaneously, because the biomass system has adhesivity, this reactor is under certain charge amount, and many materials can stick on reactor wall and blade relatively, can not effectively mix.Because this equipment stirring rake does not have the wall of scraping function, the material that sticks on the reactor wall can not in time be removed, and causes the reactor heat transfer property to descend.Obviously increased the complicacy of equipment and the difficulty of apparatus processing for strengthen steel ball or the allied equipment that mixed effect adds in cylinder in addition, be unfavorable for that industry amplifies, and noise is large during the tumbling mixer running, mixing time is long, and energy consumption is high.Therefore, for make by reproducible Biological resources production sugar fermentation become a kind of economy, competitive, can business-like method, require a kind of efficient reactor of design.
[summary of the invention]
The object of the invention is to overcome the deficiencies in the prior art, a kind of coaxial friction speed combination oar and industrial application thereof are provided.
The objective of the invention is to be achieved through the following technical solutions:
A kind of coaxial friction speed combination oar reactor, comprise round shape vertical vessel and a whipping appts that axially is arranged in container, it is characterized in that: whipping appts is the combination oar, one spirals from top to bottom at the ribbon oar stirring rake of the stir shaft periphery that is positioned at reactor center, one is positioned near the lower floor's stirring rake in reactor lower part position, a bottom stirring rake that is positioned at reactor bottom.
Described ribbon impeller is fixed on stir shaft by support bar, and spirals from top to bottom at the stir shaft periphery, consists of framework;
Described ribbon impeller is single ribbon impeller, is the hurricane band of banded plate formation.
The diameter D1 of described single ribbon impeller and the ratio of reactor diameter T are: D1: T=0.9-0.98: 1.
The ratio of the diameter D1 of the pitch P of described single ribbon impeller and ribbon impeller is: P: D1=0.5～2.5: 1.
The ratio of the height H of described ribbon impeller and diameter D1 is: H: D1=0.5～1.5: 1.
Described lower floor stirring rake is turbine/aerofoil profile stirring rake;
Described turbine/aerofoil profile stirring rake is placed in the framework that ribbon impeller forms, and is fixed on the stir shaft between two ends up and down of described ribbon impeller;
Described turbine/aerofoil profile stirring rake is straight leaf vane wheel oar, oblique leaf oar or aerofoil profile oar.
The diameter d of described turbine/aerofoil profile stirring rake is 0.3～0.7 times of ribbon impeller diameter D1.
Described aerofoil profile oar expanded area ratio is 0.3～0.9: 1.
The ratio S of interval S between described turbine/aerofoil profile stirring rake and ribbon impeller diameter D1: D1=0.3～0.5: 1.
Described bottom stirring rake is fixed on the bottom of stir shaft.
The diameter D2 of described bottom stirring rake and the ratio of reactor diameter T are: D2: T=0.9-0.98: 1.
Described ribbon impeller, turbine/aerofoil profile stirring rake can rotate with friction-motion speed;
The application of a kind of coaxial friction speed combination oar reactor in the simultaneous saccharification and fermentation of biomass production ethanol; Have biomass than high dry matter content under lytic enzyme and saccharomycetic effect, with the method for biomass saccharification fermentation ethanol processed and the reactor that adopts.
Compared with prior art, positively effect of the present invention is:
The present invention selects three kinds of different oar types, consist of the combination oar, described associated plant comprises: one spirals from top to bottom at the ribbon oar of stir shaft periphery, this oar is sheared by force and the axial main body convection circulation near relying on wall, can mix material efficiently, especially for high-viscosity material, promote liquid-solid mass transfer; In addition, because the diameter of this blade is larger, blade can play the wall effect of scraping, and can effectively prevent the bonding of wall material, prevents that the reactor heat transfer property from worsening and loss of material; Near the one or more lower floor's turbine reactor lower part position/aerofoil profile stirring rakes that are positioned at, this oar makes fluid produce axial flow, is applicable to the low viscosity system, has strengthened on the one hand the axial flow of fluid, can effectively prevent solid precipitation on the other hand; A bottom stirring rake that is positioned at the reactor bottom position, this oar plays the effect of reactor bottom being scraped the end, prevents the bonding of solid precipitation and bottom material.Special performance is separately given full play in the combination of three kinds of dissimilar blades, makes the mixing of materials in reactor, solid suspension, and system reaches mixed performance preferably.
Coaxial friction speed agitatortype of the present invention comprises stir shaft, ribbon impeller, oblique leaf/turbine/aerofoil profile stirring rake and end oar;
Described ribbon impeller be fixed on the larger hollow stir shaft of diameter by support bar or the solid stir shaft of inserting from the steel basin top on, and spiral from top to bottom at the stir shaft periphery, consist of framework;
Described turbine/aerofoil profile stirring rake is placed in the framework that described ribbon impeller forms, on the solid stir shaft that is fixed on the inner solid stir shaft of hollow stir shaft between two ends up and down of described ribbon impeller or inserts from the steel basin bottom;
Term: ribbon impeller and turbine/aerofoil profile stirring rake all has detailed definition on " Handbook ofIndustrial Mixing ".
the present invention adopts three kinds of blade combinations, material is provided sheared and two kinds of effects of circulation (comprise axially with radially), under above-mentioned two kinds of mobile actings in conjunction, the assurance reactor temperature is even, the mass transfer demand and the necessary appropriateness of gas dispersion that satisfy between the interior heat transfer of reactor and liquid-solid two-phase are sheared, make the material that joins in reactor can access short mix, make the interior energy distribution of steel basin more even, energy is utilized effectively, and near can solving wall, material glues the wall problem, enhancement of heat transfer, and can prevent deposition of solids, promote uniform particles to suspend, can be widely used in having high solids content, thick liquid and comprising passes into and reacts the reaction needed of the heterogeneous system that produces proper amount of gas.The present invention is simple in structure, and structure, operating parameters are convenient to regulate, and processing and manufacturing and installation are convenient.
[description of drawings]
Fig. 1 is the overall structure schematic diagram of reactor of the present invention;
Fig. 2 is ribbon paddle structure schematic diagram;
Fig. 2 a is single ribbon paddle structure schematic diagram;
Fig. 2 b is two ribbon paddle structure schematic diagram;
Fig. 3 is turbine/aerofoil profile paddle structure schematic diagram;
Fig. 3 a is oblique leaf/aerofoil profile paddle structure side-view;
Fig. 3 b is oblique leaf/aerofoil profile paddle structure vertical view;
Fig. 3 c is that the vane wheel oar structure is surveyed view;
Fig. 3 d is vane wheel oar structure vertical view;
Fig. 4 is end paddle structure schematic diagram.
Numbering in accompanying drawing is respectively: 1 reactor, 2 whipping apptss, 201 stir shafts, 202 ribbon impellers, 203 lower floor's stirring rakes, 204 bottom stirring rakes, 205 support bars, 206 solid stir shafts, 3 foam detectors, the 4pH meter, 5 thermopairs, 6 dissolved oxygen electrodes, 7 charging openings, 8 steam jacket devices, 9 coupling mechanisms, 10 motors, 11 second motors, 12 second coupling mechanisms.
[embodiment]
The embodiment of a kind of coaxial friction speed combination oar reactor of the present invention and industrial application thereof below is provided.
See also accompanying drawing 1 to 4, a kind of coaxial friction speed combination oar reactor, comprise round shape vertical vessel and a whipping appts that axially is arranged in container, it is characterized in that: whipping appts is the combination oar, one spirals from top to bottom at the ribbon oar stirring rake of the stir shaft periphery that is positioned at reactor center, one is positioned near the lower floor's stirring rake in reactor lower part position, a bottom stirring rake that is positioned at reactor bottom.
A whipping appts 2 that axially is arranged in described reactor 1, whipping appts comprises that 202, one of a ribbon impeller that spiral around stir shaft 201 is positioned near the lower floor's stirring rake 203 that is arranged on the reactor bottom position on solid stir shaft 206 from top to bottom.
Described ribbon impeller is fixed on stir shaft by support bar 205, and spirals from top to bottom at the stir shaft periphery, consists of framework;
Described turbine/aerofoil profile stirring rake is placed in the framework of described ribbon impeller formation, on the solid stir shaft that is fixed in the hollow stir shaft between two ends up and down of described ribbon impeller a solid stir shaft or inserts from the steel basin bottom, preferably, the number of plies of turbine/aerofoil profile stirring rake is 1～3 layer; Preferably, ribbon impeller and turbine/aerofoil profile stirring rake can rotate with friction-motion speed;
Described bottom stirring rake 204 is fixed on described stir shaft bottom;
Preferably, described bottom stirring rake is oar formula or anchor formula oar, and the structure of described oar formula or anchor formula oar all has detailed description on " Handbook of Industrial Mixing ".
Preferably, described ribbon impeller is single ribbon impeller, for the hurricane band of banded plate formation, as Fig. 2 a;
Preferably, described ribbon impeller is two ribbon impellers, for the hurricane band of banded plate formation, as Fig. 2 b;
Further, described turbine/aerofoil profile stirring rake is straight leaf vane wheel oar, oblique leaf oar or aerofoil profile oar;
Being defined on " Handbook of IndustrialMixing " handbook of term " straight leaf vane wheel oar, oblique leaf oar or aerofoil profile oar " all has detailed description;
Further, the ratio of the diameter D1 of described single ribbon impeller and reactor diameter T is: D1: T=0.9-0.98;
Further, the diameter D2 of described end oar and the ratio of reactor diameter T are: D2: T=0.9-0.98;
Further, the ratio of the diameter D1 of the pitch P of described single ribbon impeller or two ribbon stirring rakes and ribbon impeller 2 is: P: D1=0.5～2.5;
Further, the diameter d of described turbine/aerofoil profile stirring rake 203 is 0.3～0.7 times of ribbon impeller 202 diameter D;
Further, described aerofoil profile oar expanded area ratio is 0.3～0.9;
Further, the ratio S of the interval S between described turbine/aerofoil profile stirring rake and ribbon impeller diameter D1: D1=0.3～0.5;
Further, the ratio of the height H of described ribbon impeller and diameter D1 is: H: D1=0.5～1.5.
Further, the ratio of the width W of described ribbon impeller and diameter D1 is: W: D1=0.05～0.18.
Described expanded area ratio refers to the ratio of impeller vane shadow area and impeller horizontal cross-sectional area.
Preferably, stir shaft is hollow stir shaft, and it is inner that solid stir shaft is positioned at hollow stir shaft;
Preferably, stir shaft is solid stir shaft, installs from the top; Stir shaft is solid stir shaft, from steel basin bottom installation;
A steam jacket device 8 that is arranged on reactor outer wall place, this device have satisfied keeps the requirement that reactor operates at a certain temperature.
A foam detector 3 of being installed by reactor head detects due to CO
2γ-ray emission causes the foam height of system foaming.
Three sensors that are arranged on respectively wall of reactor different positions place: pH meter 4, thermopair 5 and dissolved oxygen electrode 6 are used for respectively pH value in the monitoring reaction device, temperature and oxyty.
Two motors that are used for to ribbon type stirring rake and turbine/aerofoil profile stirring rake conveying capacity, it is the three-phase variable frequency motor of 2.2KW that motor is selected rated output, rotating speed and turn to and can be regulated by frequency transformer.Preferably, motor 10 vertically is arranged on above steel basin, and agitator motor 11 vertically is arranged on the support parallel with steel basin; Preferably, motor 10 vertically is arranged on above steel basin, and the second motor 11 vertically is arranged on below steel basin.
Two contactless torque coupling mechanisms that are used for measuring the stirring system watt consumption.The sensor measurement scope is: 0～50Nm, preferably, coupling mechanism 9 adopts vertical mode to be arranged on above steel basin, the upper end adopts flange to be connected with motor, the lower end adopts axle to be connected with stir shaft, the second coupling mechanism vertically is installed on the parallel support of steel basin, and the lower end adopts flange to be connected with motor, and the upper end adopts axle to be connected with stir shaft; Preferably, coupling mechanism adopts vertical mode to be arranged on above steel basin, and the upper end adopts flange to be connected with motor, the lower end adopts axle to be connected with stir shaft, the second coupling mechanism vertically is arranged on below steel basin, and the lower end is connected by flange with motor, and the upper end adopts axle to be connected with stir shaft.The torque signal computer gathers, and the current signal by 4～20mA of coupling mechanism output is converted into numerical signal through data collecting system and is input in computer.
Two tachometers that are used for measuring agitator shaft speed.In experimentation, the rotating speed of large-diameter hollow stir shaft maintains 5～120rpm, and the solid agitator shaft speed of minor diameter maintains 100～300rpm; In the differential responses stage, the size diameter blade adopts different speed ratio operations.
the biomass synchronous saccharification technique, can be in above-mentioned reactor as the maize straw preparing fuel ethanol, add the pretreated straw material with certain dry matter content (2～30%) in reactor by charging opening 7 in batches, the granularity requirements of stalk material is in 0.07～0.3mm scope, nutritive salt (potassium hydrogen phosphate with different components concentration, sal epsom, sulfate of ammoniac, yeast extraction powder or corn steep liquor) and have the cellulase that certain enzyme is lived, enzymolysis is 0～24 hour in advance, hydrolysis temperature is controlled at 45～55 ℃, regulate pH with acid or alkali and be controlled at 4.5～5.0, the apparent viscosity that react system this moment is positioned at 10～50Pas (under average shear rate 1s-1 condition), after pre-enzymolysis, access a certain amount of fermented bacterium in reactor, leavening temperature is controlled at 30～40 ℃, and fermentation period is 48～84 hours, realizes simultaneous saccharification and fermentation production ethanol.
Adopt above-mentioned method biomass material to produce ethanol, due to choose reasonable and the configuration of paddle wheel, can effectively process the biomass material with high dry matter content, realize smoothly synchronous saccharification and the fermentation of this material, and simple in structure, be conducive to industry and amplify.
The above is only the preferred embodiment of the present invention; should be pointed out that for those skilled in the art, without departing from the inventive concept of the premise; can also make some improvements and modifications, these improvements and modifications also should be considered within the scope of protection of the present invention.
Claims (10)
1. a coaxial friction speed makes up the oar reactor, comprise round shape vertical vessel and a whipping appts that axially is arranged in container, it is characterized in that, whipping appts is the combination oar, one spirals from top to bottom at the ribbon oar stirring rake of the stir shaft periphery that is positioned at reactor center, one is positioned near the lower floor's stirring rake in reactor lower part position, a bottom stirring rake that is positioned at reactor bottom.
2. a kind of coaxial friction speed combination oar reactor as claimed in claim 1, is characterized in that, described ribbon impeller is fixed on stir shaft by support bar, and spirals from top to bottom at the stir shaft periphery, consists of framework.
3. a kind of coaxial friction speed combination oar reactor as claimed in claim 1, is characterized in that, described ribbon impeller is single ribbon impeller, is the hurricane band of banded plate formation.
4. a kind of coaxial friction speed combination oar reactor as claimed in claim 1, is characterized in that, the diameter D1 of described single ribbon impeller and the ratio of reactor diameter T are: D1: T=0.9-0.98: 1;
The ratio of the diameter D1 of the pitch P of described single ribbon impeller and ribbon impeller is: P: D1=0.5～2.5: 1;
The ratio of the height H of described ribbon impeller and diameter D1 is: H: D1=0.5～1.5: 1.
5. a kind of coaxial friction speed combination oar reactor as claimed in claim 1, is characterized in that, described lower floor stirring rake is turbine/aerofoil profile stirring rake.
6. a kind of coaxial friction speed combination oar reactor as claimed in claim 5, is characterized in that, described turbine/aerofoil profile stirring rake is placed in the framework that ribbon impeller forms, and is fixed on the stir shaft between two ends up and down of described ribbon impeller.
7. a kind of coaxial friction speed combination oar reactor as claimed in claim 1, is characterized in that, described turbine/aerofoil profile stirring rake is straight leaf vane wheel oar, oblique leaf oar or aerofoil profile oar.
8. a kind of coaxial friction speed combination oar reactor as claimed in claim 1, is characterized in that, the diameter d of described turbine/aerofoil profile stirring rake is 0.3～0.7 times of ribbon impeller diameter D1;
Described aerofoil profile oar expanded area ratio is 0.3～0.9: 1;
The ratio S of interval S between described turbine/aerofoil profile stirring rake and ribbon impeller diameter D1: D1=0.3～0.5: 1.
9. a kind of coaxial friction speed combination oar reactor as claimed in claim 1, is characterized in that, described bottom stirring rake is fixed on the bottom of stir shaft;
The diameter D2 of described bottom stirring rake and the ratio of reactor diameter T are: D2: T=0.9-0.98: 1.
10. the application of a coaxial friction speed combination oar reactor in the simultaneous saccharification and fermentation of biomass production ethanol.
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| WO2016061848A1 (en) * | 2014-10-23 | 2016-04-28 | 湖南屎壳郎环境科技有限公司 | Energy-saving stirrer |
| CN106635788A (en) * | 2017-01-04 | 2017-05-10 | 上海应用技术大学 | Coaxial different-speed combined paddle reactor |
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| CN107893022A (en) * | 2017-11-23 | 2018-04-10 | 成都欧林生物科技股份有限公司 | A kind of agitating device improved structure |
| CN108603211A (en) * | 2016-02-08 | 2018-09-28 | 川崎重工业株式会社 | Using cellulose-based biomass as the enzyme process saccharified liquid manufacturing method of raw material |
| CN109046076A (en) * | 2018-07-17 | 2018-12-21 | 安徽职业技术学院 | A kind of weaving assembly line slurry stirring device |
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| CN107893022A (en) * | 2017-11-23 | 2018-04-10 | 成都欧林生物科技股份有限公司 | A kind of agitating device improved structure |
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