CN106635788A - Coaxial different-speed combined paddle reactor - Google Patents
Coaxial different-speed combined paddle reactor Download PDFInfo
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- CN106635788A CN106635788A CN201710004068.0A CN201710004068A CN106635788A CN 106635788 A CN106635788 A CN 106635788A CN 201710004068 A CN201710004068 A CN 201710004068A CN 106635788 A CN106635788 A CN 106635788A
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- 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
- C12M21/00—Bioreactors or fermenters specially adapted for specific uses
- C12M21/18—Apparatus specially designed for the use of free, immobilized or carrier-bound enzymes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
- B01F27/05—Stirrers
- B01F27/07—Stirrers characterised by their mounting on the shaft
- B01F27/074—Stirrers characterised by their mounting on the shaft having two or more mixing elements being concentrically mounted on the same shaft
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
- B01F27/80—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a substantially vertical axis
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
- B01F27/80—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a substantially vertical axis
- B01F27/90—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a substantially vertical axis with paddles or arms
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
- B01F27/80—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a substantially vertical axis
- B01F27/92—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a substantially vertical axis with helices or screws
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- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
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- C12M27/00—Means for mixing, agitating or circulating fluids in the vessel
- C12M27/02—Stirrer or mobile mixing elements
- C12M27/08—Stirrer or mobile mixing elements with different stirrer shapes in one shaft or axis
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- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
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- C12M41/00—Means for regulation, monitoring, measurement or control, e.g. flow regulation
- C12M41/02—Means for regulation, monitoring, measurement or control, e.g. flow regulation of foam
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- C12M41/00—Means for regulation, monitoring, measurement or control, e.g. flow regulation
- C12M41/12—Means for regulation, monitoring, measurement or control, e.g. flow regulation of temperature
- C12M41/18—Heat exchange systems, e.g. heat jackets or outer envelopes
- C12M41/22—Heat exchange systems, e.g. heat jackets or outer envelopes in contact with the bioreactor walls
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- C12M41/00—Means for regulation, monitoring, measurement or control, e.g. flow regulation
- C12M41/26—Means for regulation, monitoring, measurement or control, e.g. flow regulation of pH
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- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
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- C12M41/00—Means for regulation, monitoring, measurement or control, e.g. flow regulation
- C12M41/30—Means for regulation, monitoring, measurement or control, e.g. flow regulation of concentration
- C12M41/34—Means for regulation, monitoring, measurement or control, e.g. flow regulation of concentration of gas
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- C12M45/00—Means for pre-treatment of biological substances
- C12M45/09—Means for pre-treatment of biological substances by enzymatic treatment
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F2101/00—Mixing characterised by the nature of the mixed materials or by the application field
- B01F2101/44—Mixing of ingredients for microbiology, enzymology, in vitro culture or genetic manipulation
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Abstract
The invention relates to a coaxial different-speed combined paddle reactor which is used in synchronous saccharifying fermentation of biomass-based ethanol production. The reactor comprises a cylindrical vertical vessel and a stirring device axially installed in the vessel, wherein the comprises a helical ribbon type stirring paddle helically arranged around a stirring shaft from top to bottom, a lower layer stirring paddle installed on the stirring shaft near the lower part of the cylindrical vertical vessel, and a bottom stirring paddle installed at the bottom end of the stirring shaft at the bottom of the cylindrical vertical vessel. According to the invention, a three-blade combination mode is adopted, so that the effects of shearing and circulating materials are achieved; under the combined action of the above two flows, the materials added into the reactor can be quickly mixed, so that the energy consumption distribution in a stirring tank is more uniform, thereby realizing efficient utilization of energy; the reactor can solve the problem of wall sticking of the materials near the wall surface; the reactor reinforces heat transfer, promote uniform suspension of granules and is simple in structure; the structure and operation parameters can be easily adjusted; and the reactor is convenient to process, manufacture and install.
Description
Technical field
The present invention relates to a kind of biological matter reactor, is a kind of coaxial friction speed dual impellers reactor specifically.
Background technology
Developing rapidly for modern industry, sharply increases to the demand of the energy, and the energy that countries in the world today is consumed is most of
From fossil resource.Not only reserves are limited for fossil energy, and can cause substantial amounts of NOx、SO2Deng pernicious gas and CO2, first
Alkane isothermal chamber gas is discharged, so the exploitation of environment amenable renewable resource seems becoming more and more important.Alcohol fuel is used as one
Plant most promising regenerative resource increasingly to be paid close attention to by various countries.
Mainly using sugar crops (Brazil) and corn (U.S.) as raw material, its yield is subject to for the production of alcohol fuel now
The restriction of grain resource, and cost of material is up to the 40% of totle drilling cost, it is difficult to energy demand is met for a long time, is taken a long view necessary
Abundant and cheap raw material sources are found, the research of nearest this respect is concentrated mainly on lignocellulosic.Wooden fibre according to statistics
The plain raw material of dimension takes up an area the 50% of ball total biomass.Mainly include：1. it is agricultural wastes, such as wheat straw, maize straw, corncob, big
Bean dregs, bagasse etc.；2. trade waste, the such as fibrous residue in slurrying and paper mill, sawdust；3. forestry waste；4. city
Discarded object, such as waste paper, wrapping paper.The raw material and discarded object of lignocellulosic, its composition is carbohydrate aggregation, comprising
Cellulose, hemicellulose, glucan and lignin.These materials originally generally with it is various chemistry, machinery and enzyme method at
Reason mainly to discharge hexose and pentose, so as to can be useful product with after fermentation.These are processed in terms of complexity and efficiency
It is variant.
The technique of alcohol fuel is produced by cellulose, can substantially be divided into two classes, the first kind is SHF techniques, i.e. fiber
The hydrolysis of element and the fermentation of liquid glucose are carried out in different reactors；Equations of The Second Kind is the hydrolysis of SSF techniques, i.e. cellulose and is sent out
Ferment is carried out in same reactor.SSF not only simplifies process units, and because the cellulose hydrolysis rate in fermentation tank it is remote
Less than glucose fermentation speed, make the concentration of glucose in solutions and cellobiose very low, this eliminates the need for them as hydrolysis
Inhibitory action of the product to enzyme hydrolysis, can accordingly reduce the consumption of enzyme.In addition low concentration of glucose decreases miscellaneous bacteria infection
Chance.At present SSF has become up-and-coming biomass preparing alcohol technique.
By taking maize straw simultaneous saccharification and fermentation production ethanol as an example, its reaction engineering characteristic is analyzed, substantially can be summarized
For it is following some：
First, the dynamics of enzymatic hydrolysis reaction is investigated, its feature is as follows, and first enzyme must be adsorbed to cellulose surface
A few minutes, adsorbed enzyme are about the time required to (adsorbance meets Langmuir adsorption isotherms), the adsorption equilibrium process
Subsequently cellulose is acted on, initial rate is quickly, after carrying out a few minutes with hydrolysis, under hydrolysis rate is notable during effect
Drop, hydrolysis 24h after, hydrolysis rate less than initial hydrolysis rate 2%.As can be seen here, for whole hydrolytic process, though
So the time required to it very long (having technical process to be even up to several days), but most important process is that, in initial a few minutes, this is just
It is required that hydrolase, bacterial classification can quickly mix and be adsorbed onto cellulose surface in stalk material.
2nd, the ratio of the consumption of the consumption and stalk material of enzyme (bacterial classification) is investigated, is easily found, both amounts are to differ greatly
, in addition, the viscosity of hydrolase (bacterial classification) far below stalk material viscosity, for comparing the different viscous thing system that differs greatly
Mixing, its hybrid technology will be difficult many, and this is just to the feed way of material (maize straw material, hydrolase, bacterial classification)
(be disposably to add or be dividedly in some parts particularly with substantial amounts of stalk material, if being dividedly in some parts, feed time for how long, often
The amount of secondary addition is again how many), feed location, paddle mixed performance put forward higher requirement.Similarly, in reactor
The control of pH value has identical problem.
3rd, phase-state change of the maize straw material during whole diastatic fermentation is investigated, its process is as follows：In initial liquid
In the several hours changed, biomass structure is degraded, and material is gradually converted into thick starchiness by solid-state in reactor；With
Liquefaction process is deeply carried out, and the structure of maize straw is wholly absent, and material is liquid by Solid State Transformation；In follow-up saccharification and
In sweat, the viscosity of material continues to reduce, and after the completion of reaction, material is in slurry or suspension liquid shape in reactor.This
Outward, in sweat, system has CO2Gas is produced, and now system is gas-liquid-solid three-phase complex system.As can be seen here, for
SSF techniques, in same reactor, the viscosity of system experienced and adhere to low viscous dynamic transition process by height, and this requires set
The saccharification reactor of meter can have preferable mixed performance in the different viscosities stage.Reaction later stage, the suspension of solid phase, product
The discharge of raw gas is also the problem that must take into.
4th, front to address, cellulase must be adsorbed onto first cellulose surface and just can be hydrolyzed reaction, from mass transfer angle
Degree, the granularity of stalk material is less, and it is bigger with the contact area of cellulase, then hydrolysis effect is better.This is just to being added to
Stalk raw meal particle size proposes certain requirement in reactor.
5th, for saccharification and fermentation reaction, need to maintain what is carried out at a certain temperature, for the optimal temperature of saccharification reaction
, at 45～55 DEG C, the optimum temperature of fermentation reaction is at 28～33 DEG C for degree.This will appropriate design reactor jacket and reactor
Heating operation mode, makes reactor heat transfer property disclosure satisfy that reaction needs.
In order to perform above-mentioned technique, various equipment have been used in different types of biomass, carry out different
Process, including small-scale process exploitation and some full-scale plants.The kind of some equipment has been used, including interval
Stirred reactor (Gusakov and Sinitsyn, 1985Enz.Microb.Technol.7:346-352,
CN101090962A, CN101160388A), continuous stream stirred reactor (US4257818), griding reaction device (Ryu and Lee
(1983)Biotechnol.Bioeng.25:53-65) extruding reaction device (US6176176), NREL shrink bed (shrinking
Bed) reactor (Lee et al., 2001, Appl.Biochem.Biotech.91-93:331-340) stir with electromagnetic field inducing reinforcement
Dynamic reactor (Gusakov et al., (1996) Appl.Biochem.Biotech.56：141-153).
Above-mentioned reactor, in addition to Chinese patent CN101090962A, the reactor of other relatively early stages is suitable for hydrolyzing respectively
And zymotechnique, type of reactor mostly is hydrolysis process device, focuses on the grinding to cellulose substances more its structure, to increase
The contact area of hydrolase and cellulose, strengthens hydrolysis effect, and it is excessively complicated to have thus resulted in reactor inner member, is unfavorable for work
Industry.Chinese patent CN101160388A discloses a kind of equipment for processing biomass, and the equipment has and is connected in container
The rotatable baffle plate of side, abrasive media (comprising free floating the reaction vessel interior pill) it is and anti-for conveying processing
Answer the injection lance of the device of agent.The equipment is equally only applicable to hydrolysis process, and device structure is excessively complicated, is unfavorable for industry
Change.Chinese patent CN101090962A combines enzyme hydrolysis and relies on ensuring that mechanical force (mainly shearing force and tear edge) and apply
For the mixed type of the gravity principle of biomass, filled from such as drum mixer, tilting concrete mixer or similar mixing
The free fall mixers put, the primarily radial gravity diffusion mixing of its mixing principle, axial convection current is less.Simultaneously as raw
Substance system has adhesiveness, and under certain charge, relatively large number of material can stick to reactor wall to the reactor
And on blade, it is impossible to effectively mixed.Wall function is scraped because the equipment paddle does not have, reactor wall is sticked to
On material can not be removed in time, cause reactor heat transfer property decline.In addition add in cylinder to strengthen mixed effect
Steel ball or similar device obviously increase equipment the processing of complexity and equipment difficulty, be unfavorable for industrial amplification, and roll
Noise is big when mixer operates, and incorporation time is long, high energy consumption.Therefore, in order that being fermented by the production of reproducible living resources
Sugar becomes a kind of economic, competitive, commercially viable method, it is desirable to design a kind of efficient reactor.
The content of the invention
It is an object of the invention to overcome the deficiencies in the prior art, there is provided a kind of coaxial friction speed dual impellers reactor.
The purpose of the present invention is achieved through the following technical solutions：
A kind of coaxial friction speed dual impellers reactor, produces in the simultaneous saccharification and fermentation of ethanol, the reactor for biomass
Comprising cylindrical shape vertical vessel and an axially mounted agitating device in a reservoir, the agitating device includes one from upper
Lower wall is spun on the axial ribbon impeller of stirring, and one is located near cylindrical shape vertical vessel lower position installed in stirring
Lower floor's paddle on axle；One is located at the bottom paddle that cylindrical shape vertical vessel bottom is arranged on shaft bottom.
Described ribbon impeller is fixed on shaft by support bar, and is spiraled from top to bottom in shaft week
Side, constitutes framework.
Described ribbon impeller is single ribbon impeller of the hurricane band being made up of banded plate.
The ratio of the diameter D1 and reactor diameter T of described ribbon impeller is：
D1:T=0.9-0.98：1；The ratio of the pitch P of described ribbon impeller and the diameter D1 of ribbon impeller
Example be：P: D1=0.5～2.5：1；The ratio of the height H and diameter D1 of described ribbon impeller is：H:D1=0.5～
1.5：1.
Described lower floor's paddle is turbine/aerofoil profile paddle；Described turbine/aerofoil profile paddle is placed in helical-ribbon type stirring
In the framework that oar is formed, it is fixed on the shaft up and down between two ends of the ribbon impeller.
The ratio of the diameter D2 and reactor diameter T of described bottom paddle is：D2:T=0.9-0.98：1.
Described turbine/aerofoil profile paddle is straight leaf vane wheel oar or oblique leaf oar or Aerofoil impeller；Described turbine/aerofoil profile stirring
The diameter d of oar is 0.3～0.7 times of ribbon impeller diameter D1；Described Aerofoil impeller disk ratio is 0.3～0.9：1；It is described
Turbine/aerofoil profile paddle between interval S and ribbon impeller diameter D1 ratio S:D1=0.3～0.5：1.
The shaft is made up of hollow shaft and solid shaft, and solid shaft is located inside hollow shaft,
Hollow shaft is fixedly connected ribbon impeller, and solid shaft is fixedly connected lower floor's paddle；Hollow shaft and solid
Shaft connects respectively motor, makes ribbon impeller, lower floor's paddle have different stirring rotary speeies.
The shaft is made up of two solid shafts, and a solid shaft connects spiral shell from after reactor head loading
Ribbon blender oar, another solid shaft connects lower floor's paddle, two solid shafts from after the loading of reactor chamber bottom
Motor is connect respectively, makes ribbon impeller, lower floor's paddle that there are different stirring rotary speeies.
One steam jacket device is installed, for maintaining what reactor was operated at a certain temperature at the reactor outer wall
Require；The reactor head installs foam detector, produces the foam for causing system to foam by CO2 gases for detection high
Degree；Various location is respectively provided with pH meter, thermocouple and dissolved oxygen electrode in the wall of reactor, is respectively intended to monitor reactor
Interior pH value, temperature and oxyty.
Compared with prior art, the invention has the beneficial effects as follows：
The present invention selects three kinds of different paddle type, constitutes dual impellers, and the combination unit includes：One spirals from top to bottom
In the ribbon oar of shaft periphery, the oar, can be efficiently to material by near wall Strong shear and axial main body convection circulation
Mixed, particularly with high-viscosity material, promoted liquid-solid mass transfer；Further, since the blade is relatively large in diameter, blade can play
Wall effect is scraped, the bonding of wall material can be effectively prevented, prevents reactor heat transfer property from deteriorating and loss of material；One more
Individual lower floor's turbine/aerofoil profile paddle near reactor lower part position, the oar makes fluid produce axially flowing, it is adaptable to low
Viscosity thing system, on the one hand strengthens the axial direction flowing of fluid, on the other hand can effectively prevent solid precipitation；One is located at reaction
The bottom paddle of device bottom position, the oar plays a part of to scrape bottom to reactor bottom, prevents solid precipitation and bottoms material
Bonding.The combination of three kinds of different type blades, gives full play to respective special performance, mixes the material in reactor, Gu
Body suspends, and system reaches preferable mixed performance.
The present invention is made for two kinds there is provided shearing to material using three kinds of blade combinations with circulation (including axially and radially)
With under the collective effect of above two flowing, it is ensured that reactor temperature is uniform, heat transfer and liquid-solid two-phase in reactor are met
Between the necessary appropriateness shearing of mass transfer demand and gas dispersion, the material being added in reactor is quickly mixed
Close, make that energy distribution in tank diameter is more uniform, energy is utilized effectively, and can solve the problem that the viscous wall of near wall material is asked
Topic, augmentation of heat transfer, and can prevent solid from depositing, and promote particle even suspension, can be widely applied to high solids content, viscous fluid
Body and comprising be passed through and react produce proper amount of gas multiphase thing system reaction needs.Present configuration is simple, structure, operation
Parameter is easy to adjust, and processing and manufacturing and installation are facilitated.
Description of the drawings
Fig. 1 is the general structure schematic diagram of the coaxial friction speed dual impellers reactor of the present invention；
Fig. 2 is ribbon paddle structure schematic diagram；
Wherein：A () is single ribbon paddle structure schematic diagram, be (b) double ribbon paddle structure schematic diagrames；
Fig. 3 is turbine/Aerofoil impeller structural representation；
Wherein：A () is oblique leaf/Aerofoil impeller structural side view, (b) be oblique leaf/Aerofoil impeller structure top view, (c) is turbine
Paddle structure surveys view, (d) is vane wheel oar structure top view；
Fig. 4 is end oar structural representation.
Specific embodiment
Below in conjunction with the accompanying drawings invention is described further with embodiment.
As shown in figure 1, the coaxial friction speed dual impellers reactor 1 of the present invention, including agitating device 2, shaft 201, ribbon
Formula paddle 202, lower floor's paddle 203, bottom paddle 204, support bar 205, solid shaft 206, foam detector 3,
PH meter 4, thermocouple 5, dissolved oxygen electrode 6, charge door 7, steam jacket device 8, the first coupler 9, the first motor 10, the second motor
11st, the second coupler 12.Agitating device 2 is axially mounted in reactor 1, and agitating device 2 spirals from top to bottom including one
Ribbon impeller 202 around shaft 201, one is located near reactor bottom position installed in solid shaft 206
On lower floor's paddle 203.Ribbon impeller 202 is fixed on shaft 201 by support bar 205, and disk from top to bottom
Shaft periphery is spun on, framework is constituted.Lower floor's paddle 203 is turbine/aerofoil profile paddle, and turbine/aerofoil profile paddle is placed in institute
In the framework that the ribbon impeller 202 stated is formed, the hollow between two ends up and down of ribbon impeller 202 is fixed on
A solid shaft 206 or from the stirring solid shaft 206 inserted of trench bottom in shaft, it is preferred that turbine/aerofoil profile
The number of plies of paddle is 1～3 layer；Preferably, ribbon impeller can be rotated with turbine/aerofoil profile paddle with friction speed.
Bottom paddle 204 is fixed on shaft bottom.
Term：Ribbon impeller and turbine/aerofoil profile paddle exist《Handbook of Industrial Mixing》On
There is detailed definition.
Preferably, the bottom paddle exists for the structure of paddle or anchor formula oar, such as Fig. 4, the paddle or anchor formula oar
《Handbook of Industrial Mixing》On be described later in detail.
Preferably, described ribbon impeller is single ribbon impeller, is the hurricane band that banded plate is constituted,
Such as Fig. 2 a.
Preferably, described ribbon impeller is double ribbon impellers, is the hurricane band that banded plate is constituted,
Such as Fig. 2 b.
Further, the turbine/aerofoil profile paddle be straight leaf vane wheel oar, such as Fig. 3 c, Fig. 3 d, oblique leaf oar or Aerofoil impeller, such as
Fig. 3 a, Fig. 3 b.
Term " straight leaf vane wheel oar, oblique leaf oar or Aerofoil impeller " is defined on《Handbook of Industrial
Mixing》It is described later in detail on handbook.
Further, the ratio of the diameter D1 and reactor diameter T of described single ribbon impeller is：D1:T=0.9-
0.98。
Further, the ratio of the diameter D2 and reactor diameter T of described end oar is：D2:T=0.9-0.98.
Further, the pitch P of described single ribbon impeller or double ribbon paddles is straight with ribbon impeller 2
The ratio of footpath D1 is：P: D1=0.5～2.5.
Further, the diameter d of the turbine/aerofoil profile paddle 203 is the 0.3～0.7 of the diameter D of ribbon impeller 202
Times.
Further, described Aerofoil impeller disk ratio is 0.3～0.9.
Further, between the turbine/aerofoil profile paddle interval S and ratio S of ribbon impeller diameter D1:D1=
0.3～0.5.
Further, the ratio of the height H and diameter D1 of the ribbon impeller is：H:D1=0.5～1.5.
Further, the ratio of the width W and diameter D1 of the ribbon impeller is：W:D1=0.05～0.18.
The disk ratio refers to the ratio of impeller blade projected area and impeller horizontal cross-sectional area.
Preferably, shaft is hollow shaft, and solid shaft is located inside hollow shaft.
Preferably, shaft is solid shaft, is installed from top；Shaft is solid shaft, from stirring trench bottom
Install.
One steam jacket device 8 being arranged at reactor outer wall, the device meets maintenance reactor in a constant temperature
The requirement of the lower operation of degree.
One foam detector 3 installed by reactor head, detects due to CO2Gas produces the bubble for causing system to foam
Foam height.
Three sensors for being separately mounted to wall of reactor various location：PH meter 4, thermocouple 5 and dissolved oxygen electrode 6,
It is respectively intended to monitor pH value, temperature and oxyty in reactor.
Two motors for being used to convey energy to ribbon type paddle and turbine/aerofoil profile paddle, motor selects specified work(
Rate is the three-phase variable frequency motor of 2.2KW, and rotating speed and steering can be adjusted by frequency converter.Preferably, the first motor 10 is vertically installed at
Tank diameter top, the second motor 11 is vertically installed on the support parallel with tank diameter；Preferably, the first motor 10 is vertically-mounted
Above tank diameter, the second motor 11 is vertically installed at tank diameter lower section.
Two contactless torque couplers for being used for measuring stirring system power consumption.Sensor measurement range is：0～
50Nm, it is preferred that the first coupler 9 is arranged on tank diameter top using vertical mode, upper end is connected with motor using flange, under
End is connected with shaft using axle, and it is that on the parallel support of tank diameter, lower end adopts with motor that the second coupler is vertically-mounted
Flange connects, and upper end is connected with shaft using axle；Preferably, coupler is arranged on tank diameter top using vertical mode, on
End is connected with motor using flange, and lower end is connected with shaft using axle, and the second coupler 12 is vertically installed at tank diameter lower section,
Lower end is connected with motor by flange, and upper end is connected with shaft using axle.Torque signal computer is acquired, by coupler
The current signal of 4～20mA of output, Jing data collecting systems are converted into numerical signal and are input in computer.
Two tachometers for being used for measuring agitator shaft speed.In experimentation, large-diameter hollow shaft turn
Speed maintains 5～120rpm, and the solid agitator shaft speed of minor diameter maintains 100～300rpm；Differential responses stage, size diameter
Blade is not using at the same speed than operation.
Biomass synchronous saccharification technique, such as maize straw preparing fuel ethanol can be in above-mentioned reactors, by 7 points of charge door
Criticize and the pretreated straw material with certain dry matter content (2～30%) is added into reactor, the granularity of stalk material will
Ask in the range of 0.07～0.3mm, nutritive salt (potassium hydrogen phosphate, magnesium sulfate, sulfate of ammoniac, yeast extract with different component concentration
Take powder or corn steep liquor) and the cellulase with certain enzyme activity, digesting 0～24 hour in advance, hydrolysis temperature is controlled 45～55
DEG C, with acid or alkali pH controls are adjusted 4.5～5.0, now the apparent viscosity of reactant system (is averagely cut positioned at 10～50Pas
Cutting speed rate 1s-1Under the conditions of)；After pre- enzymolysis, a certain amount of fermented bacterium is accessed into reactor, fermentation temperature is controlled 30～40
DEG C, fermentation period is 48～84 hours, realizes that simultaneous saccharification and fermentation produces ethanol.
Biomass material production ethanol with the aforedescribed process is adopted, due to reasonable selection and the configuration of agitator arm, can be effective
Biomass material of the process with high dry content, smoothly realize the synchronous saccharification of the material and fermentation, and simple structure,
Be conducive to industrial amplification.
Claims (10)
1. a kind of coaxial friction speed dual impellers reactor, produces in the simultaneous saccharification and fermentation of ethanol, the reactor bag for biomass
Vertical vessel containing cylindrical shape and an axially mounted agitating device in a reservoir（2）, it is characterised in that：The agitating device
（2）Spiral from top to bottom including one and stirring axial ribbon impeller (202), one is located at cylindrical shape vertical vessel
The lower floor's paddle (203) being arranged near lower position on shaft；One is arranged on positioned at cylindrical shape vertical vessel bottom
The bottom paddle (204) of shaft bottom.
2. coaxial friction speed dual impellers reactor according to claim 1, it is characterised in that：Described ribbon impeller
(202) it is fixed on shaft by support bar (205), and is spiraled from top to bottom in shaft periphery, constitutes framework.
3. coaxial friction speed dual impellers reactor according to claim 1, it is characterised in that：Described ribbon impeller
(202) be the hurricane band being made up of banded plate single ribbon impeller.
4. coaxial friction speed dual impellers reactor according to claim 1, it is characterised in that：Described ribbon impeller
(202) diameter D1 and the ratio of reactor diameter T be：D1:T=0.9-0.98：1；The pitch P of described ribbon impeller
It is with the ratio of the diameter D1 of ribbon impeller：P: D1=0.5 ~ 2.5：1；The height H of described ribbon impeller with it is straight
The ratio of footpath D1 is：H: D1=0.5~1.5：1.
5. coaxial friction speed dual impellers reactor according to claim 1, it is characterised in that：Described lower floor's paddle
(203) it is turbine/aerofoil profile paddle；Described turbine/aerofoil profile paddle is placed in the framework of ribbon impeller formation, fixed
On the shaft up and down between two ends of the ribbon impeller (202).
6. coaxial friction speed dual impellers reactor according to claim 1, it is characterised in that：Described bottom paddle it is straight
The ratio of footpath D2 and reactor diameter T is：D2:T=0.9-0.98：1.
7. coaxial friction speed dual impellers reactor according to claim 5, it is characterised in that：Described turbine/aerofoil profile stirring
Oar is straight leaf vane wheel oar or oblique leaf oar or Aerofoil impeller；The diameter d of described turbine/aerofoil profile paddle is ribbon impeller diameter
0.3～0.7 times of D1；Described Aerofoil impeller disk ratio is 0.3 ~ 0.9：1；Interval S between described turbine/aerofoil profile paddle
With ratio S of ribbon impeller diameter D1:D1=0.3 ~ 0.5：1.
8. according to the arbitrary described coaxial friction speed dual impellers reactor of claim 1-7, it is characterised in that：The shaft
(201) it is made up of hollow shaft and solid shaft, solid shaft is located inside hollow shaft, and hollow shaft is fixed
Connection ribbon impeller (202), solid shaft is fixedly connected lower floor's paddle (203)；Hollow shaft and solid stirring
Axle connects respectively motor, makes ribbon impeller (202), and lower floor's paddle (203) is with different stirring rotary speeies.
9. according to the arbitrary described coaxial friction speed dual impellers reactor of claim 1-7, it is characterised in that：The shaft
(201) it is made up of two solid shafts, a solid shaft connects ribbon impeller from after reactor head loading
(202), another solid shaft connects lower floor's paddle (203), two solid shafts from after the loading of reactor chamber bottom
Motor is connect respectively, ribbon impeller (202) is made, and lower floor's paddle (203) is with different stirring rotary speeies.
10. according to the arbitrary described coaxial friction speed dual impellers reactor of claim 1-7, it is characterised in that：Outside the reactor
One steam jacket device is installed at wall（8）, for the requirement for maintaining reactor to operate at a certain temperature；The reactor top
Portion is installed by foam detector（3）, the foam height for causing system to foam is produced by CO2 gases for detection；The reactor device
Various location is respectively provided with pH meter on wall（4）, thermocouple（5）And dissolved oxygen electrode（6）, it is respectively intended to monitor pH in reactor
Value, temperature and oxyty.
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| CN201710004068.0A CN106635788A (en) | 2017-01-04 | 2017-01-04 | Coaxial different-speed combined paddle reactor |
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| CN107115806A (en) * | 2017-06-15 | 2017-09-01 | 太和县美欣药业有限公司 | A kind of medicine material processing agitating device |
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| CN110621395B (en) * | 2017-05-10 | 2022-07-26 | 艾卡多搅拌及混合工程有限公司 | Stirring element device |
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| CN107115806A (en) * | 2017-06-15 | 2017-09-01 | 太和县美欣药业有限公司 | A kind of medicine material processing agitating device |
| CN107159077A (en) * | 2017-06-16 | 2017-09-15 | 安徽机电职业技术学院 | A kind of asphalt production reactor |
| WO2019114275A1 (en) * | 2017-12-12 | 2019-06-20 | 陈军瑞 | Enzymatic hydrolysis apparatus with fixing mechanism |
| CN108435777A (en) * | 2018-04-08 | 2018-08-24 | 丰桢敏 | A kind of contaminated soil pyrolysis spray prosthetic device |
| CN109247606A (en) * | 2018-11-28 | 2019-01-22 | 山东宇冠机械有限公司 | A kind of molasses adding set |
| CN109453941A (en) * | 2018-12-17 | 2019-03-12 | 青岛科技大学 | A kind of feeding, stirring, discharging, coating integrated device |
| CN109453941B (en) * | 2018-12-17 | 2023-10-31 | 青岛科技大学 | Feeding, stirring, discharging and coating integrated device |
| US11717800B2 (en) | 2019-04-24 | 2023-08-08 | Applied Materials, Inc. | Reactor for coating particles in stationary chamber with rotating paddles |
| CN111117675B (en) * | 2020-01-07 | 2021-03-19 | 山东理工大学 | Sectional spiral stirring type biomass pyrolysis liquefaction system |
| CN111117675A (en) * | 2020-01-07 | 2020-05-08 | 山东理工大学 | Sectional spiral stirring type biomass pyrolysis liquefaction system |
| WO2022026732A1 (en) * | 2020-07-30 | 2022-02-03 | Applied Materials, Inc. | Paddle configuration for a particle coating reactor |
| CN112226340A (en) * | 2020-09-30 | 2021-01-15 | 安徽恒天环保装备科技有限公司 | Aerobic fermentation container with coaxial different-speed stirring structure |
| CN112526115A (en) * | 2020-12-14 | 2021-03-19 | 中建西部建设西南有限公司 | Device and method for rapidly measuring solid content of concrete waste slurry |
| CN112526115B (en) * | 2020-12-14 | 2022-11-22 | 中建西部建设西南有限公司 | Device and method for quickly measuring solid content of concrete waste slurry |
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