CN205948877U - Reactor device - Google Patents
Reactor device Download PDFInfo
- Publication number
- CN205948877U CN205948877U CN201620668461.0U CN201620668461U CN205948877U CN 205948877 U CN205948877 U CN 205948877U CN 201620668461 U CN201620668461 U CN 201620668461U CN 205948877 U CN205948877 U CN 205948877U
- Authority
- CN
- China
- Prior art keywords
- heat transfer
- agitator
- frustum
- transfer element
- reactor
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Abstract
The utility model discloses a reactor device belongs to bioengineering, chemical engineering and environmental engineering field. The utility model discloses a reactor device's mixing system's main part comprises multiunit radial flow agitator and the combination of multiunit axial flow agitator. The heat transfer unit (HTU) has the water conservancy diversion function concurrently in the jar, through its rational arrangement of, combines the water conservancy diversion effect of frustum of a cone side perforated sieve board and a lot of gas -liquid dispersing action of radial flow agitator, and mass transfer process and heat transfer process organic integration are link up each other to messenger reactor's heat transfer unit (HTU) and the flow field that mixing system produced. Air distributor is arranged to the multiple spot in reaction vessel, has both promoted the gas -liquid dispersion, again further circulation flow and the mix of strengthening the reaction flow field. The utility model discloses overcome the dispersion of high strength gas -liquid and heat among the solid reactor device of extensive gas -liquid and gas -liquid and remove and be difficult to the problem that satisfies simultaneously, can be at extensive gas -liquid and gas -liquid high -efficient mass transfer of realization and heat transfer process in the reactor admittedly.
Description
Technical field
The utility model is related to a kind of reactor assembly, belongs to bioengineering, Chemical Engineering and field of environment engineering.
Background technology
Gas-liquid two-phase dispersion and mixing are widely used in the processes such as ventilating fermentation, oxidation reaction, hydrogenation, bio-aeration
Unit.The device enabling the gentle liquid-solid reaction of gas-liquid at present mainly has：Bubble tower, airlift reactor, stirred tank reactor
With aeration tank etc..In ventilating fermentation process and biotransformation, the application of ventilation stirred tank reactor is extremely widespread.
Chemical reaction or aerobe reaction that either gas-liquid two-phase participates in, Gas-Liquid Dispersion process is usually associated with biography
Thermal process, in small-scale reactor device, diabatic process tends not to become technical bottleneck, and engineer increasingly focuses on gas-liquid
Dispersion efficiency.But during large scale fermentation, the heat transfer area that can install with the increase of reactor volume, unit volume
Become little, often make reaction heat (metabolic heat) effectively removes the technical bottleneck becoming scaling -up.Lead in high-cell density
In wind sweat, the heating strength that cell metabolism produces can reach 30kW/m3Zymotic fluid；Heat transfer area needed for unit volume
Even up to 3.0m2/m3Zymotic fluid, this high intensity heat transfer requirement hardly results in full in conventional extensive ventilation fermentation tank
Foot.
The outer heat transfer unit (HTU) of common tank has：Ordinary unit chuck, the monoblock type chuck with spiral stream guidance band, semicircle pipe clamp
Set, Honeycomb Jacket, channel-type chuck etc..In common tank, heat transfer unit (HTU) has：Vertical coil pipe, king bolt coil pipe, spring disk
Pipe etc..
Specifically, on a small scale (<10m3) and medium-scale (10～100m3) ventilation bioreactor in, for meet
Efficient heat transfer demand in course of reaction, typically arranges coil pipe in setting chuck and tank outside tank simultaneously.With typically middle isotactic
As a example mould ventilation fermentation tank, the heat transfer area of unit volume is in 1.2～2.0m2/m3Between zymotic fluid scope, in extensive (＞
100m3) in ventilation fermentation tank, the heat transfer area of unit volume is difficult more than 2.0m2/m3Zymotic fluid.Increasing with reactor volume
Greatly, the outer installable chuck area of tank is very limited, therefore becomes increasingly dependent on and installs more coil pipes in tank, lead to coil pipe it
Between gap become little, and then affect flow rate in tank for the fluid, mixing, mass transfer and heat transfer efficiency.
Although vertical coil pipe is with the function of plate washer, suitable coil pipe quantity and density are conducive to the mass transfer in tank and biography
Thermal process, but the increase with reactor volume, coil device increasingly extends to tank central area, between paddle and coil pipe
Little away from becoming, wide plate washer function can be unfavorable for the performance of agitator dispersion and mixed function on the contrary；Gap between coil pipe becomes
Little, even less than 30～50mm, this will have a strong impact on effect and the uniformity of tank inner transmission matter and heat transfer.
Because the cooling water in king bolt coil pipe and spring coil pipe can drain completely, therefore in the sterilizing of fermentation tank
Steam consumption can be saved in journey, but after reactor volume increases, the pitch between coil pipe becomes little, the gap between coil pipe is very
To less than 30～50mm, this different subregions that will lead to be formed in reactor：The abundant turbulent area at tank center, spring coil pipe
Stagnant area between the inside stagnant area, king bolt coil pipe and the wall that surround etc., the mass transfer in stagnant area and heat transfer efficiency are low,
Overall flow field in reactor is in highly non-uniform property.
Because extensive gas-liquid gentle liquid-solid reactor device volume is huge, integral device often cannot be transported, and typically needs
Each part of reactor is manufactured respectively and is transported, then carry out scene processing in owner location and assemble.Due to stirring
Mix the complex nature of the problem, stirring system manufacture manufactures often to be come by different manufacturers from reaction vessel (inclusion heat transfer unit (HTU))
Complete, therefore easily cause the different understanding to mass transfer and heat transfer, lead to reactor mass transfer and diabatic process efficiency can not and
Turn round and look at.The design and fabrication technology of the extensive gentle liquid-solid reactor of gas-liquid still depends on the experience of each manufacturing enterprise at present,
Continue to use design and the manufacturing philosophy of medium-scale reactor, not enough to the new problem understanding occurring in commercial scale reactor, lack
Effectively solution and measure.
Utility model content
For solving the above problems, the utility model considers from the overall structure of reactor, ingenious arrangement heat transfer unit (HTU), ventilation
Pipe and locus in reactor for the diversion member, and the Spatial Coupling of difference in functionality paddle, make heat transfer unit (HTU) and stir
The flow field insertion mixing system generation is merged, provide a kind of for efficient mass transfer in the gentle liquid-solid reactor of extensive gas-liquid and
The solution of heat transfer and apparatus.The utility model adopts the part of reactor assembly to form with common response device basic phase
With, but effectively optimize its space structure and combination, so that Gas-Liquid Dispersion, heat transfer and mixing efficiency is significantly improved, have relatively
Low power consumption, plays the effect improving reactivity worth and saving energy consumption.
The utility model provides a kind of reactor assembly, is to be suitable for efficient mass transfer, the extensive gas-liquid of heat transfer and gas-liquid
Solid reactor assembly, also apply be applicable in medium scale gas-liquid gentle liquid-solid reactor device.
Described reactor assembly mainly includes reaction vessel, stirring system, heat transfer unit (HTU), guiding device, air sparger；
The main body of described stirring system is made up of multigroup radial flow agitator and multigroup axially stream stirrer combination, wherein said radial flow
Agitator includes bottom agitator, 1～3 middle part radial flow agitator；The heat transfer unit (HTU) being installed on reaction vessel interior is by many
Group cylindric heat transfer element arranged in co-axial alignment composition；Described air sparger includes different spatial arrangement in reaction vessel
Multigroup breather pipe and frustum of a cone side porous sieve plate；Described frustum of a cone side porous sieve plate is arranged in the cylinder of reaction vessel
Portion, has 1～3；The lower surface diameter of described frustum of a cone side porous sieve plate and reaction vessel equal diameters, upper surface diameter exists
Between 0.5～1.0D；Wherein D is the diameter of reaction vessel interior cylindrical shape heat transfer element.
In one embodiment, the described heat transfer unit (HTU) being installed on reaction vessel interior is coaxial by cylindric heat transfer element
Rearrange.
In one embodiment, described cylindrical shape heat transfer element can be compact arranged king bolt coil pipe it is also possible to
It is built-in Honeycomb Jacket or channel-type chuck.
In one embodiment, described cylindric heat transfer element diameter (D) and the ratio of reaction vessel internal diameter (T) exist
Between 0.5～0.9.
In one embodiment, between 30～125mm, group inner disc ligament exists the caliber of described king bolt coil pipe
Between 0～50mm.
In one embodiment, the middle part radial flow agitator of described stirring system and frustum of a cone side porous sieve plate one
One coupling, setting 1～3 is right, and middle part radial flow agitator is arranged on directly over the porous sieve plate of corresponding frustum of a cone side.
In one embodiment, described middle part radial flow agitator, its diameter (dM) with reaction vessel internal diameter (T) it
Than between 0.15～0.5.
In one embodiment, the radial flow agitator in described stirring system can be Rushton agitator, arrow leaf
Disk stirrer, CD-6 agitator, BT-6 agitator or other radial flow agitator, can be multigroup identical agitator groups
Close or multigroup difference stirrer combination.
In one embodiment, the axial direction stream agitator in described stirring system can be four oblique leaf open type agitators,
Screw, three wide leaf propeller mixers, four wide leaf propeller mixers, three narrow leaf propeller mixers, four narrow leaf rotary propeller types
Agitator and other similar axial direction stream agitators, can be multigroup identical stirrer combinations or multigroup difference is stirred
Mix device combination.
In one embodiment, the group number of described radial flow agitator is the group number axially flowing agitator between 1～3
Between 3～8 groups.
In one embodiment, the ratio of stirrer diameter (d) and reaction vessel internal diameter (T) is between 0.2～0.5.
In one embodiment, the ratio of stirrer diameter (d) and cylindric heat transfer element diameter (D) 0.3～0.6 it
Between.
In one embodiment, different stirrer diameter can be identical or different.
In one embodiment, the ratio of adjacent agitator spacing (M) and stirrer diameter (d) is between 1.5～3.
In one embodiment, the stirring of stirring system can be constant speed stirring or stepless speed regulation stirring, stirs
Mix rotating speed can according to depending on the OUR of reaction system it is also possible to according to the oxygen dissolving value feedback control of reaction system and regulation.
In one embodiment, in described reactor assembly, the type of agitator, locus, diameter and cylindrical shape
Between the installation site of heat transfer element, cylindric heat transfer element diameter, group, spacing cooperates, bottom agitator and the middle part frustum of a cone
Agitator near the porous sieve plate of side mostly is radial flow agitator, and other agitators mostly are axially stream agitator.Cylindric biography
The group spacing of thermal element is to control the important parameter of fluid guiding, in reactor the latter half, organizes spacing (CB) preferably little, its spacing
Between 0～100mm, play increase heat transfer area, simultaneously work as being locally isolated the function of bubbling area and stirring area, but close
During the frustum of a cone of middle part frustum of a cone side porous sieve plate, middle part cylindrical shape heat transfer element spacing CMNeed sufficiently large, be 0.4～
1.6dM, fluid could be directed to below the radial flow agitator at middle part, promote gas-liquid flow to produce twice dispersing effect.In
The top of portion's radial flow agitator, can arrange multilayer and axially flow agitator, can be upper-turn-type or press-down type
It is also possible to setting press-down type and upper-turn-type agitator from bottom to top.If press-down type and the combination of upper-turn-type, this combination and institute
State space between cylindric heat transfer element group to mate one by one and laterally aligned；Then in this combination laterally corresponding cylindrical shape heat transfer element
Group spacing (CU) preferably wider, its spacing is in 0.2～0.8dMBetween, the gas-liquid polyphase flow being beneficial near wall region enters stirring area simultaneously
Generation circulates, and strengthens gas-liquid mass transfer and diabatic process.
In one embodiment, described cylindrical shape heat transfer element, when being arranged at reactor the latter half, cylindric heat transfer
Spacing C between the group of elementBBetween 0～100mm；When near the frustum of a cone of middle part frustum of a cone side porous sieve plate, middle part
Spacing C between cylindric heat transfer element groupMFor 0.4～1.6dM；Wherein dMDiameter for middle part radial flow agitator.
In one embodiment, the top setting multilayer of described middle part radial flow agitator axially flows agitator, two
Cylindric heat transfer element group spacing C between personUIn 0.2～0.8dMBetween；Wherein dMDiameter for middle part radial flow agitator.
In one embodiment, in the gentle liquid-solid reactor device of described extensive gas-liquid, shaft can be overall
Axle or multistage shaft are formed by connecting；Can be solid shafting or hollow shaft；The mounting means of shaft can
To be single span formula or multi-point support installation.
In one embodiment, the tubular heat transfer element in described reactor has the effect of guiding device concurrently.
In reactor, heat transfer unit (HTU) is made up of multigroup cylindrical shape heat transfer element arranged in co-axial alignment, can increase heat transfer area and heat transfer
Efficiency, has diversion function concurrently；Cylindric heat transfer element gap number between group and spacing are close with the flow field flow direction of stirring system
Cut distribution closes, and so that fluid is constituted in tank and circulates.When described cylindrical shape heat transfer element is king bolt coil pipe, the king bolt in group
Closely, gap is between 0～30mm for coil arrangements.
In common ventilation fermentation tank, tube pitch ratio larger (50～150mm) of inner coil pipe, fluid is only through inner coil pipe
Gap, the effective mass transfer of guarantee and heat transfer, but so allow for the installable heat transfer area of unit volume and be restricted,
Can there are multiple Stagnation zones unavoidably therefore after scaling -up.The utility model adopts multigroup coaxial mounted cylindric heat transfer
Element, increased the heat transfer area installed in commercial scale reactor, improves heat-transfer intensity, meanwhile, cylindric heat transfer
Element also serves as guiding device, no stagnant area in fermentation tank, enhances the circulation mixing of gas-liquid mass transfer.
In one embodiment, described multigroup breather pipe includes the first breather pipe and the second breather pipe.
In one embodiment, described first breather pipe is arranged on immediately below bottom agitator.
First breather pipe is arranged on immediately below bottom agitator, such mounting means, and the air being passed through can be made to carry out
High efficiency dispersion, forms tiny bubble.Bottom agitator is arranged near the lower surface of reaction vessel cylinder, with reaction container bottom
Spacing (B) be 0.25～0.5T, the diameter (d of bottom agitatorB) it is 0.3 with the ratio of the diameter (D) of cylindric heat transfer element
～0.5, the bottom face of the cylindric heat transfer element in one group of bottom is less than cylinder lower surface, the spacing with bottom agitator mounting plane
For 0.1～0.4dBBetween.
In one embodiment, uniform aperture above described first breather pipe, between 4～20mm, aperture is total in aperture
The ratio of area and ventilation tube section is between 0.5～1.0.Preferably, described ventilation bottom of the tube arranges several outages, aperture
Between 4～20mm.
In one embodiment, described second breather pipe is arranged on the cylindric heat transfer unit of the near-bottom of reaction vessel
Between part periphery and reaction vessel wall.
In one embodiment, uniform aperture above described second breather pipe, between 4～20mm, aperture is total in aperture
The ratio of area and ventilation tube section is between 0.2～0.5.Ventilation bottom of the tube arranges several outages, and aperture is in 4～20mm
Between.
In one embodiment, in the middle part of the reaction vessel cylinder of described reactor assembly, 1～3 frustum of a cone side is set
Face porous sieve plate, between 20～60 °, between 15～40%, aperture is between 5～30mm for porosity at the base angle of the frustum of a cone.
In one embodiment, the arrangement mode of the sieve aperture of described frustum of a cone side porous sieve plate can be rectangle row
Row, square arrangement, diamond array, equilateral triangle arrangement.The lower surface diameter of sieve plate is equal with container diameter, and its upper surface is straight
Footpath is less than or equal to cylindric heat transfer element diameter D, can be 0.5～1.0D.
In one embodiment, the circular cone platform upper surface of described frustum of a cone side porous sieve plate and adjacent cylinders thereon
The distance between shape heat transfer element lower surface is in 0.2～0.8dMBetween；Wherein dMDiameter for middle part radial flow agitator.
In one embodiment, described frustum of a cone side porous sieve plate can be integral type it is also possible to split type,
Installed with facilitating and safeguard.Sieve plate can be directly welded on wall, it would however also be possible to employ gripper shoe is indirectly connected with.Sieve plate bottom with
A fixed gap is left, to prevent hydrops and to be easy to clean between wall.
In space between the second breather pipe and frustum of a cone side porous sieve plate, the effect of Gas-Liquid Dispersion is similar to bubbling
Tower, from the second breather pipe, bubble out mutually collides and coalescence in uphill process, and pressure reduces in addition, and bubble is increasingly
Greatly, mass-transfer efficiency declines.In the middle part of cylinder, the mesh of setting porous sieve plate is：(1) sieve aperture can be split again to air pocket
And dispersion, reduce bubble diameter；(2) play diversion function, biphase gas and liquid flow is guided to the suction of middle part radial flow agitator
Area, carries out twice dispersing by this agitator to bubble, reduces bubble diameter, improves bubble motion speed, lifts Gas-Liquid Dispersion
Efficiency and mass-transfer efficiency.
In one embodiment, described multigroup breather pipe also includes the 3rd breather pipe, and described 3rd breather pipe is arranged on
Between cylindric heat transfer element on the circular cone platform of frustum of a cone side porous sieve plate and wall.
In one embodiment, the middle part radial flow agitator of described reactor assembly, its installation site can be with circle
Cylindric heat transfer element lower surface on cone platform side porous sieve plate is concordantly it is also possible to be higher than under this cylindric heat transfer element
End face.Position between the cylindric heat transfer element on circular cone platform and reactor wall, can install the 3rd breather pipe with
Strengthen ventilation intensity and the gas-liquid dispersion efficiency of reactor near wall region, simultaneously facilitate and circulate, conduct heat and mixing efficiency.Also may be used
Not install breather pipe, the gas-liquid two-phase flow of twice dispersing or gas-liquid-solid three phase flow that middle part radial flow agitator produces, profit
The shunting action being produced with the relative installation of cylindric heat transfer element lower surface and middle part radial flow agitator, makes one
Divide the space that gas-liquid two-phase flow or gas-liquid-solid three-phase flow between cylindric heat transfer element and reactor wall, another part
Two-phase flow or gas-liquid-solid three phase flow enter cylindric heat transfer element inside region (stirring area), make the heat transfer unit (HTU) in reactor
The flow field being produced with stirring system is mutually communicated, and mass transport process and diabatic process organically blend.
In one embodiment, each breather pipe of described reactor assembly can be horizontally mounted it is also possible to keep micro-
Little gradient (0.005～0.01), be beneficial to cleaning, the operation such as sky disappears when can drain liquid in pipe.
In one embodiment, in described reactor assembly, the caliber of the second breather pipe and the 3rd breather pipe, passage
Size, quantity can identical it is also possible to different；According to local features in reactor assembly, depending on circulation time.3rd
Breather pipe can be single group or multigroup, between 1～3 group in reactor assembly.Ventilation bottom of the tube is provided with discharge opeing
Hole.
In one embodiment, in described reactor assembly, guiding device also includes plate washer, and baffle plate setting meets full shelves
Slat element, in reactor assembly, the quantity in different vertical region for the plate washer can be identical or different.Plate washer number
Amount is between 4～10 pieces, and plate washer is arranged on inside cylindric heat transfer element.
In one embodiment, described reaction vessel is in tall and thin type, and its ratio of height to diameter is between 2.5～6.So favourable
In improving bubble residence time, increase the heat transfer area installed of unit volume, be conducive to mass transfer and heat transfer efficiency.
In one embodiment, the shell portion of described reaction vessel can be straight tube shape or upper part
Local bulkiness type.
In one embodiment, the material of described reaction vessel can be the suitable of carbon steel, stainless steel or other high intensity
Preferably material.The upper and lower end socket of reaction vessel can be ellipse head or dished (torispherical) head.Upper and lower end socket can be according to production
Technique needs to arrange various adapters, the mouth of pipe and auxiliary equipment.At reaction vessel top, 1 manhole can be set or at top, bottom
Portion respectively sets 1 manhole, can arrange helper in reactor, to install, cleaning and to overhaul.
In one embodiment, described reactor assembly also includes auxiliary device, such as manhole, the support of bearing, cylinder
Shape heat transfer element support, outlet, charging aperture, material-feeding port, inoculation mouth, helper, male flange etc..
In one embodiment, described reactor assembly also includes external jacket, and described external jacket can be monoblock type folder
Set, any one such as the monoblock type chuck with spiral stream guidance band, Agitated Vessel With Half-pipe-coil Jacket, Honeycomb Jacket, channel-type chuck.
The beneficial effects of the utility model：
(1) reactor assembly of the present utility model plays the built-in heat transmission function of cylindric heat transfer element and water conservancy diversion simultaneously
Function, carries out space optimization with the agitator of difference in functionality in stirring system in reactor and combines, make the heat transfer in reactor
The flow field that device is produced with stirring system is mutually communicated fusion, both improves the heat transfer area installed and the biography of unit volume
The thermal efficiency, enhances Gas-Liquid Dispersion and the mass-transfer efficiency of reactor again.
(2) reactor assembly of the present utility model arranges air sparger in different spaces multiple spot, introduces in regional area
The advantageous characteristic of bubble tower, is integrated with the gas-liquid twice dispersing work(of frustum of a cone side porous sieve plate and middle part radial flow agitator
Can, so that no stagnant area in reactor is existed, you can to overcome the bubble coalescence process of bubbling area, further to strengthen reactive flowfield
Circulate and dispersion efficiency.
(3) reactor assembly of the present utility model has the characteristics that dispersion efficiency is high, heat transfer is fast, energy consumption is low, can be applicable to
In the extensive course of reaction such as ventilating fermentation, hydrogenation, oxidation reaction, it is capable of efficient mass transfer and diabatic process.
Brief description
Fig. 1：Reactor assembly schematic diagram；Wherein, 1 first breather pipe, 2 second breather pipes, 3 bottom agitators, 4 second layers
Agitator, 5 cylindric heat transfer elements (king bolt coil pipe), 6 third layer agitators, 7 first intermediate bearing supports, 8 frustum of a cone sides
Face porous sieve plate, 9 middle part radial flow agitators, 10 layer 5 agitators, 11 plate washers, 12 layer 6 agitators, in the middle of 13 second
The support of bearing, 14 shafts, 15 frames, 16 drive systems, 17 mechanical seals, 18 manholes, 19 first shaft couplings, 20 semicircle pipe clamps
Set, 21 second bearings, 22 second shaft couplings, 23 the 3rd breather pipes, 24 3rd bearings, 25 cylinders, 26 clutch shaft bearings, 27 discharges
Mouth, 28 skirts；
Fig. 2：Frustum of a cone side porous sieve plate block diagram；Wherein, 29 sieve apertures, 30 delivery holes；
Fig. 3：Frustum of a cone side porous sieve plate block diagram；Wherein, 8 frustum of a cone side porous sieve plate；
Fig. 4：Reaction vessel interior component top view；Wherein, 1 first breather pipe, 2 second breather pipes, 5 cylindric heat transfer units
Part (king bolt coil pipe), 11 plate washers, 20 Agitated Vessel With Half-pipe-coil Jackets, 25 cylinders, 31 breeder tubes；
Fig. 5：Cylindric heat transfer element (built-in cellular formula chuck) block diagram；Wherein, 32 cooling water inlet/outlet pipes, 33 circles
Tubular base plate, 34 bulging plates；
Fig. 6：Cylindric heat transfer element (built-in cellular formula chuck) block diagram；
Fig. 7：Cylindric heat transfer element (built-in cellular formula chuck) block diagram；
Fig. 8：Reactor assembly flow field schematic diagram, wherein, 35 stirring area, 36 bubbling areas.
Specific embodiment
Embodiment 1：Reactor assembly
As shown in figure 1, the reactor assembly involved by the utility model include reaction vessel, stirring system, heat transfer unit (HTU),
Guiding device, air sparger and some auxiliary equipments.
Reaction vessel is made up of cylinder 25, upper cover, low head, skirt 28.
Stirring system is by multigroup agitator, shaft 14, bearing, shaft coupling, mechanical seal 17, frame 15 and drive system
16 compositions.Described multigroup agitator includes bottom agitator 3, second layer agitator 4, third layer agitator 6, middle part radial flow stir
Mix device 9, layer 5 agitator 10, layer 6 agitator 12.Described bearing has 3, including clutch shaft bearing 26, second bearing 21,
3rd bearing 24.Described shaft coupling has 2, including first shaft coupling 19, second shaft coupling 22.
Heat transfer system is made up of the outer Agitated Vessel With Half-pipe-coil Jacket 20 of tank, cylindric heat transfer element 5.
Guiding device is made up of cylindric heat transfer element 5, frustum of a cone side porous sieve plate 8, plate washer 11.
Air sparger is by the first breather pipe 1, the second breather pipe 2, the 3rd breather pipe 23 and frustum of a cone side porous sieve plate 8
Composition.
Auxiliary device also includes manhole 18, the first intermediate bearing support 7, the second intermediate bearing support 13, outlet 27, enters
Material mouth, material-feeding port, helper, male flange etc..
As shown in figure 1, the large-scale reactor assembly involved by the utility model, the ratio of height to diameter ratio of its reaction vessel is larger,
Upper and lower end socket can be ellipse head or dished (torispherical) head, for supporting the devices such as the motor and speed reducer of stirring system,
End socket can be carried out thickening and strengthen it is also possible to increase support strength by installing stiffening ring；The support pedestal one of reaction vessel
As be skirt.Outside reaction vessel middle cylinder body 25, heat transfer unit (HTU) also can be installed, can be with monoblock type chuck, with spiral stream guidance band
The combination of any one or more of patterns such as monoblock type chuck, Agitated Vessel With Half-pipe-coil Jacket, Honeycomb Jacket, channel-type chuck, with honeycomb
Formula chuck, channel-type chuck are preferred, and the cost performance using Agitated Vessel With Half-pipe-coil Jacket is higher.
Bottom agitator 3 is generally radial flow agitator, is preferred with BT-6 agitator, the diameter (d of bottom agitator 3B)
Between 0.2～0.5T, there is the first breather pipe 1 immediately below this agitator, the function of bottom agitator 3 is that high efficiency dispersion is passed through
Air, forms minute bubbles.This agitator 3 is arranged near the lower surface of cylinder, and the spacing (B) with reaction container bottom is 0.25
～0.5T, the bottom face of the king bolt coil pipe of near-bottom is less than between bottom agitator 3, and bottom agitator 3 mounting plane
Away from for 0.1～0.4dBBetween.First ventilation bottom of the tube arranges several outages, and aperture is between 4～20mm.
Second and third layer of agitator (4,6) is axially to flow agitator from bottom to top, can be four oblique leaf open type agitators, spiral shell
Rotation oar, three wide leaf propeller mixers, four wide leaf propeller mixers, three narrow leaf propeller mixers, four narrow leaf rotary propeller types stir
Mix device and other similar axial direction stream agitators, can be multigroup identical stirrer combination or multigroup different stirring
Device combines.For conventional low viscosity zymotic fluid, it is preferred with four wide leaf propeller mixers, the diameter (d) of agitator and reaction
The ratio of inside diameter of vessel (T) is between 0.2～0.5, and the ratio of inner coil pipe screw diameter (D) is between 0.3～0.6.Agitator is straight
Footpath can be identical or different.The ratio of adjacent agitator spacing (M) and stirrer diameter (d) 1.5～3 it
Between.
The stirring of stirring system can be constant speed stirring or stepless speed regulation stirring, and speed of agitator can be according to reaction
It is also possible to according to the oxygen dissolving value feedback control of reaction system and regulation depending on the OUR of system.
In reactor, heat transfer unit (HTU) is made up of multigroup cylindrical shape heat transfer element arranged in co-axial alignment, and described cylindrical shape heat transfer element can
To be compact arranged king bolt coil pipe or built-in Honeycomb Jacket or channel-type chuck.Described cylindric heat transfer
The group number of element and heat transfer area determine according to heat transfer requirement and the mounting condition of real reaction process.
Described cylindrical shape heat transfer element is when being king bolt coil pipe, the king bolt coil arrangements in group closely, gap 0～
Between 50mm.The caliber of king bolt coil pipe, between 30～125mm, typically adopts the seamless steel pipe of standard, outer surface is carried out
Polishing.
The ratio of the diameter (D) of cylindric heat transfer element and reaction vessel internal diameter (T), can be according to biography between 0.5～0.9
Heat demand and installing space position are adjusted.
As shown in figure 1, in the middle part of the cylinder 25 of reactor assembly, 1 frustum of a cone side porous sieve plate 8 of setting, such as Fig. 2～
Shown in Fig. 3, the base angle of the frustum of a cone, between 20～60 °, is preferred with 30 °；Porosity, between 15～40%, is preferred with 25%；
Between 5～30mm, the arrangement mode of sieve aperture 29 is preferred with equilateral triangle arrangement in the aperture of sieve aperture 29.The many hole sizers in frustum of a cone side
Plate 8 can be integral type it is also possible to split type, with manufacture and mounting condition is adaptable.Sieve plate can directly weld
It is connected on wall it is also possible to be indirectly connected with wall with gripper shoe.Leave a fixed gap between sieve plate bottom and wall, referred to as lead
Fluid apertures 30, to prevent hydrops and to be easy to clean.Screen-aperture is different because the solid phase particles size in reaction system is different, if
Carry out cell or saccharomycetes to make fermentation, sieve aperture and delivery hole size can be smaller, if carry out mould and actinomycete fermentation, its hole
Footpath needs larger more particularly suitable.
As shown in figure 4, cylindric heat transfer element (king bolt coil pipe) 5 peripheries near reaction container bottom and wall it
Between arrange the second breather pipe 2, the uniform breeder tube 31 in the second breather pipe 2 top, between 4～20mm, conventional is low viscous in aperture
It is preferred with 10mm under the conditions of degree zymotic fluid, the ratio of the aperture gross area and ventilation tube section is between 0.2～0.5, is preferred with 0.3.
Ventilation bottom of the tube arranges several outages, and aperture is between 4～20mm.
As shown in Fig. 5～7, the cylindric heat transfer element in reaction vessel can also be built-in Honeycomb Jacket, by justifying
Tubular base plate 33, bulging plate 34 and cooling water inlet/outlet pipe 32 form.It is usually by two blocks of plain plates (cylindric base plate 33, bulging
Plate 34) linked together by laser welding and form the weld zone with certain geometrical shape, relend and help bulging shaping side
Method is so as to the bulging plate 34 in his non-solder area deforms, thus forming closed convex arc shaped cavity folder between two blocks of steel plates
Set.Cooling water inlet/outlet pipe 32 may be mounted at inner side or the outside of cylindric heat transfer element, is installed as good with inner side.For convenience of clear
Clean and prevent microbiological contamination risk, the surface of cylindric heat transfer element is processed by shot blasting.
As illustrated in figures 1 and 8, the frustum of a cone side porous sieve plate 8 of reactor assembly is with middle part radial flow agitator 9 one by one
Coupling, is set to 1 right in this example.Middle part radial flow agitator 9 installation site can with circular cone platform on cylindrical shape
Heat transfer element lower surface is concordantly it is also possible to be higher than this cylindric heat transfer element lower surface.Cylindric biography on circular cone platform
Position between thermal element and wall, installs the 3rd breather pipe 23 to strengthen ventilation intensity and the gas-liquid dispersion efficiency of near wall region,
Simultaneously facilitate and circulate, conduct heat and mixing efficiency.Diameter (the d of middle part radial flow agitator 9M) and reaction vessel internal diameter (T)
Ratio between 0.15～0.5, be preferred with 0.3.
As illustrated in figures 1 and 8, the group spacing of cylindric heat transfer element is to control the important parameter of fluid guiding, in reaction
Device the latter half, organizes spacing (CB) preferably little, its spacing, between 0～50mm, plays increase heat transfer area, simultaneously work as local every
From the function of bubbling area 36, but when near the middle part frustum of a cone, middle part cylindrical shape heat transfer element spacing CMNeed sufficiently large, be 0.4
～1.6dM, fluid could be directed to below the radial flow agitator at middle part, promote gas-liquid flow to produce twice dispersing effect.?
The top of middle part radial flow agitator, can arrange multilayer and axially flow agitator, can be upper-turn-type or press-down type
It is also possible to the combined type of setting press-down type and upper-turn-type agitator from bottom to top, cylindric heat transfer element group between the two
Spacing (CU) preferably wider, its spacing is in 0.2～0.8dMBetween, the gas-liquid polyphase flow being beneficial near wall region enters stirring area 35 simultaneously
Generation circulates, and strengthens gas-liquid mass transfer and diabatic process.
Shaft 14 can be overall axle or multistage shaft is formed by connecting；Can be solid shafting or
Hollow shaft；The mounting means of shaft can be single span formula or multi-point support is installed.
Plate washer 11 setting meets full plate condition, and in reactor assembly, the quantity in different vertical region for the plate washer can be phase
Same or different.Plate washer quantity is between 4～10 pieces, and plate washer is arranged on inside cylindric heat transfer element.
Embodiment 2：Reactor assembly
With 200m3As a example ventilation fermentation tank, effectively dress liquid amasss and is about 150m3, using scheme described in the utility model, such as
Shown in Fig. 1, the cylinder 25 internal diameter (T) of reaction vessel is 4000mm, a height of 14600mm of cylinder；Upper cover and low head are ellipse
Circle end socket；For Φ 76 × 3.5 semi-circular tube spiral welded in container outer surface, semi-circular tube pitch is 110mm to external jacket, from cylinder
End face arranges external jacket to liquid level, and external jacket heat transfer area is about 90m2；The cylindric heat transfer unit of reaction vessel interior
Part doubles as diversion member, for the king bolt coil pipe being closely wound, using Φ 76 × 3 seamless steel pipe, appearance mirror polish, screw diameter
(D) it is 3500mm, pitch is 76mm, king bolt coil pipe arranged in co-axial alignment is installed, and heat transfer area is about 358m2, therefore reactor dress
The total heat exchange area put is 448m2；First group of king bolt coil pipe lower surface and cylinder from bottom to top near reaction container bottom
Lower surface is concordant, the spacing (C between the corresponding king bolt coil pipe group of radial flow agitator 9 in the middle part of reaction vesselM) it is 800mm, instead
Answer the laterally corresponding king bolt coil pipe that in container top half, top upper-turn-type agitator 12 is combined with press-down type agitator 10
Spacing (C between groupU) it is 400mm, the spacing (C between other king bolt coil pipe groupsB) it is 51mm；Bottom agitator 3 is BT-6 type footpath
To stream agitator, its diameter (dB) it is 1300mm, middle part radial flow agitator 9 is BT-6 type, its diameter (dM) with for 1100mm,
Axially stream agitator has 4 layers, and its diameter (d) is 1100mm, and bottom agitator 3 away from reaction container bottom spacing (B) is
2000mm, the spacing (M) between all agitators is 1750mm, and press-down type and upper-turn-type agitator are four wide leaf rotary propeller types and stir
Mix device, flow direction is contrary.
The lower surface diameter of frustum of a cone side sieve tray 8 is equal with reaction vessel diameter (T), and installation site is in the reactor
Portion, the spacing (C of its neighbouring two groups of king bolt coil pipeM) it is 800mm, frustum of a cone side sieve tray 8 and the first jackshaft can be met
Hold the installing space demand of support 7, the base angle of the frustum of a cone is 30 °, a diameter of 5mm of sieve aperture 29, and porosity is 20%, and sieve aperture is arranged
Mode for cloth is equilateral triangle, and a diameter of 3000mm in frustum of a cone upper surface, therefore frustum of a cone height are 288.7mm.Delivery hole 30
A size of 50 × 15, quantity is 120, uniform in frustum of a cone side bottom.Plate washer is installed on the inner side of king bolt coil pipe, width
For 280mm, quantity is 6 pieces, uniformly, highly for 11000mm.First ventilation duct 1 of reactor, the second ventilation duct 2, third venting
The nominal diameter of pipe 7 is respectively DN150, DN100 and DN80, and the centerline diameter of the first ventilation duct 1 is 600mm, the second ventilation
The centerline diameter of pipe 2 and third venting pipe 7 is 3750mm, and the admission pressure of ventilation duct is 4atm.Reaction vessel wall thickness, drive
Dynamic system 16, shaft 14, shaft coupling, mechanical seal, the support of bearing, king bolt coil pipe supporting stand, frustum of a cone side sieve tray prop up
Frame, manhole 18, helper and various adapter etc. are designed by the requirement of common ventilation fermentation tank and determine.
Using the utility model scheme, its heat transfer area is up to 448m2, heat transfer area per unit volume is 2.99m2/m3Fermentation
Liquid, no stagnant area in fermentation tank, the uniformity of mass transfer and heat transfer is significantly better than conventional ventilation fermentation tank.
Equally with cumulative volume as 200m3Ventilation fermentation tank as a example, effectively dress liquid amasss and is about 150m3, routinely design
Vertical coil pipe is installed in ventilation fermentation tank, total heat conduction area is about 250m2, heat transfer area per unit volume is 1.67m2/m3Fermentation
Liquid, now built-in coil space is only 30mm, obvious to the retardation of fluid, and the volume in stagnant area (or low flow velocity area) is about
For 18m3, account for general assembly liquid amass 12%, the therefore mass transfer in vertical coil pipe area and heat transfer efficiency is severely impacted, and leads to
Reactor flow field distributing inhomogeneity.
Embodiment 3：Cylindric heat transfer element
Similar with the reactor assembly described in embodiment 2, the heat transfer element outside the reaction vessel in embodiment 2 is changed into
For Honeycomb Jacket, the cylindric heat transfer element of reaction vessel interior also changes into as Honeycomb Jacket.As shown in Fig. 5～7, built-in
Cylindric heat transfer element cylindrical, all no any covering of upper/lower terminal, also serve as heat transfer element and diversion member.Wherein
The internal diameter of cylindric base plate 33 is 3500mm, and the height of cylindric base plate 33 is adjusted according to the installation site of reactor agitating device
Whole it is also possible to height with reference to king bolt coil pipe in embodiment 2；The thickness of cylindric base plate 33 is 4～6mm, bulging plate 34
Nominal thickness is not less than 1mm, in the present embodiment, is preferred with 1.2mm, a diameter of 16mm of Laser Welding contact, and spacing is 75mm,
Bulging height is 6mm.Cooling water inlet/outlet pipe 32 is installed on inside Honeycomb Jacket, and cylindric base plate 33 is in inner side elder generation and cooling water
Branch pipe welding, is then connected to cooling water inlet/outlet pipe 32, finally passes to outside reaction vessel, is preferred with welding manner.
The heat transfer area of the outer Honeycomb Jacket of the tank of the reaction vessel in the present embodiment is up to 130m2, honeycomb fashion in tank
Chuck arranged in co-axial alignment, heat transfer area is 228m2, dress liquid is long-pending to be about 150m3, heat transfer area per unit volume is 2.39m2/m3Fermentation
Liquid is although the heat transfer area per unit volume of this example is slightly below embodiment 2, but still the fermentation tank (1.67m far above conventional design2/
m3Zymotic fluid).Secondly as the heat transfer coefficient of Honeycomb Jacket is 1.3～1.6 times of king bolt coil pipe, therefore adopt honeycomb
The scheme of formula chuck is still better than king bolt coil pipe.Third, when adopting Honeycomb Jacket, the cylindric heat transfer element table in reactor
Face smooth it is easy to cleaning, and microbiological contamination risk can be greatly reduced.
Said apparatus form be the utility model preferred embodiment, but form of the present utility model be not limited to that it is allowed to
Make modification within the specific limits.
Although the utility model is open as above with preferred embodiment, it is not limited to the utility model, any
Person skilled in the art, without departing from spirit and scope of the present utility model, can do various changes and modification, therefore originally
The protection domain of utility model should be by being defined that claims are defined.
Claims (10)
1. a kind of reactor assembly is it is characterised in that described reactor assembly mainly includes reaction vessel, stirring system, heat transfer
Device, guiding device, air sparger；The main body of described stirring system is by multigroup radial flow agitator and multigroup axially stream stirring
Device combination is constituted, and wherein said radial flow agitator includes bottom agitator, 1～3 middle part radial flow agitator；It is installed on anti-
The heat transfer unit (HTU) within container is answered to be made up of multigroup cylindrical shape heat transfer element arranged in co-axial alignment；Described air sparger is included in reaction
Multigroup breather pipe of different spatial arrangement and frustum of a cone side porous sieve plate in container；Described frustum of a cone side porous sieve plate
It is arranged in the middle part of the cylinder of reaction vessel, have 1～3；The lower surface diameter of described frustum of a cone side porous sieve plate is held with reaction
Device equal diameters, upper surface diameter is between 0.5～1.0D；Wherein D is the diameter of reaction vessel interior cylindrical shape heat transfer element.
2. a kind of reactor assembly according to claim 1 is it is characterised in that the middle part radial flow of described stirring system stirs
Mix device to mate one by one with frustum of a cone side porous sieve plate, middle part radial flow agitator is in corresponding frustum of a cone side porous sieve plate just
Top.
3. a kind of reactor assembly according to claim 1 is it is characterised in that the base angle of the described frustum of a cone is at 20～60 °
Between, between 15～40%, aperture is between 5～30mm for porosity.
4. a kind of reactor assembly according to claim 1 is it is characterised in that the circle of described frustum of a cone side porous sieve plate
Vertical range between cone platform upper surface and thereon adjacent cylinders shape heat transfer element lower surface is in 0.2～0.8dMBetween；Wherein
dMDiameter for middle part radial flow agitator.
5. a kind of reactor assembly according to claim 1 is it is characterised in that described multigroup breather pipe includes the first ventilation
Pipe and the second breather pipe；Described first breather pipe is arranged on immediately below bottom agitator；Described second breather pipe is arranged on reaction
Between the cylindric heat transfer element periphery of the near-bottom of container and reaction vessel wall.
6. a kind of reactor assembly according to claim 5 is it is characterised in that uniformly little above described first breather pipe
Hole, between 4～20mm, the ratio of the aperture gross area and ventilation tube section is between 0.5～1.0 in aperture.
7. a kind of reactor assembly according to claim 1 is it is characterised in that described multigroup breather pipe also includes threeway
Tracheae, described 3rd breather pipe is arranged on cylindric heat transfer element and device on the circular cone platform of frustum of a cone side porous sieve plate
Between wall.
8. a kind of reactor assembly according to claim 1, it is characterised in that described cylindrical shape heat transfer element, is arranged at
Spacing C during reactor the latter half, between the group of cylindric heat transfer elementBBetween 0～100mm；Near the middle part frustum of a cone
Spacing C during the frustum of a cone of side porous sieve plate, between the cylindrical shape heat transfer element group of middle partMFor 0.4～1.6dM；Wherein dMFor middle part
The diameter of radial flow agitator.
9. a kind of reactor assembly according to claim 1 is it is characterised in that the top of described middle part radial flow agitator
Setting multilayer axially flows agitator, cylindric heat transfer element group spacing C betweenUIn 0.2～0.8dMBetween；Wherein dM
Diameter for middle part radial flow agitator.
10. a kind of reactor assembly according to claim 1 it is characterised in that described cylindric heat transfer element straight
The ratio of the internal diameter of footpath and reaction vessel is between 0.5～0.9.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620668461.0U CN205948877U (en) | 2016-06-30 | 2016-06-30 | Reactor device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620668461.0U CN205948877U (en) | 2016-06-30 | 2016-06-30 | Reactor device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN205948877U true CN205948877U (en) | 2017-02-15 |
Family
ID=57969099
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201620668461.0U Active CN205948877U (en) | 2016-06-30 | 2016-06-30 | Reactor device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN205948877U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105944647A (en) * | 2016-06-30 | 2016-09-21 | 江南大学 | Large-scale gas-liquid and gas-liquid-solid reactor device with efficient mass transfer and heat transfer |
-
2016
- 2016-06-30 CN CN201620668461.0U patent/CN205948877U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105944647A (en) * | 2016-06-30 | 2016-09-21 | 江南大学 | Large-scale gas-liquid and gas-liquid-solid reactor device with efficient mass transfer and heat transfer |
| CN105944647B (en) * | 2016-06-30 | 2017-11-17 | 江南大学 | A kind of efficient mass transfer, the gentle liquid-solid reactor device of extensive gas-liquid of heat transfer |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN106552560B (en) | A kind of airlift reactor with spiral porous sieve plate | |
| WO1996020041A1 (en) | An agitated reactor | |
| CN105944647B (en) | A kind of efficient mass transfer, the gentle liquid-solid reactor device of extensive gas-liquid of heat transfer | |
| CN208066329U (en) | A kind of microvesicle formula gas-liquid reactor and system | |
| CN201342325Y (en) | Mixer | |
| WO2018094621A1 (en) | Wastewater biochemical treatment device | |
| CN208667710U (en) | A kind of full-automatic magnetic agitation stainless steel fermentation tank | |
| CN205948877U (en) | Reactor device | |
| CN208839593U (en) | A kind of glass-lined reactor | |
| CN201864727U (en) | Novel air-lift internal loop reactor | |
| CN203944382U (en) | Liquid-phase reactor | |
| CN108404700B (en) | Airlift type rotary circulation mixing device without inner guide cylinder | |
| CN212316105U (en) | Medium-sized high mass transfer circulating type ventilation fermentation tank | |
| CN201990659U (en) | Fermentation tank | |
| CN206157148U (en) | Antibiotic fermentation cylinder | |
| CN201372231Y (en) | Wastewater up-flow anaerobic sludge bed reactor | |
| CN210787321U (en) | Stirring reaction kettle | |
| CN210473843U (en) | Stirring system for compound fertilizer production | |
| CN210357184U (en) | Coil pipe in synthetic kettle and synthetic kettle | |
| CN207313581U (en) | A kind of new bio fermentation tank | |
| CN207872144U (en) | A kind of reaction unit being used to prepare big proportion and bulky grain crystal | |
| CN206188811U (en) | Homogeneity fermentation cylinder | |
| CN2920389Y (en) | Polyisobutylene polymerization kettle | |
| CN213222146U (en) | Novel high-speed rotary reactor | |
| CN214881414U (en) | Bioreactor |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |