CN108554335B - Mixed fluid stirring mechanism and tubular reactor - Google Patents
Mixed fluid stirring mechanism and tubular reactor Download PDFInfo
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- CN108554335B CN108554335B CN201711471893.8A CN201711471893A CN108554335B CN 108554335 B CN108554335 B CN 108554335B CN 201711471893 A CN201711471893 A CN 201711471893A CN 108554335 B CN108554335 B CN 108554335B
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- 238000003756 stirring Methods 0.000 title claims abstract description 273
- 239000012530 fluid Substances 0.000 title claims abstract description 22
- 230000007246 mechanism Effects 0.000 title claims abstract description 19
- 239000000463 material Substances 0.000 claims description 55
- 239000000376 reactant Substances 0.000 claims description 19
- 230000004323 axial length Effects 0.000 claims description 3
- 238000011010 flushing procedure Methods 0.000 claims 1
- 238000006243 chemical reaction Methods 0.000 description 23
- 230000000694 effects Effects 0.000 description 17
- 238000007789 sealing Methods 0.000 description 9
- 239000012257 stirred material Substances 0.000 description 6
- 230000009471 action Effects 0.000 description 4
- 238000013461 design Methods 0.000 description 4
- 238000000034 method Methods 0.000 description 4
- 230000004048 modification Effects 0.000 description 4
- 238000012986 modification Methods 0.000 description 4
- 239000002994 raw material Substances 0.000 description 4
- 230000005484 gravity Effects 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 230000000712 assembly Effects 0.000 description 2
- 238000000429 assembly Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000010907 mechanical stirring Methods 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 238000013019 agitation Methods 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000005192 partition Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/18—Stationary reactors having moving elements inside
- B01J19/1812—Tubular reactors
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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
-
- 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
- B01F27/11—Stirrers characterised by the configuration of the stirrers
- B01F27/114—Helically shaped stirrers, i.e. stirrers comprising a helically shaped band or helically shaped band sections
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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
- B01F27/11—Stirrers characterised by the configuration of the stirrers
- B01F27/19—Stirrers with two or more mixing elements mounted in sequence on the same axis
-
- 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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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0006—Controlling or regulating processes
- B01J19/0013—Controlling the temperature of the process
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0053—Details of the reactor
- B01J19/0066—Stirrers
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00051—Controlling the temperature
- B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
- B01J2219/00076—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements inside the reactor
- B01J2219/00081—Tubes
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
- Mixers Of The Rotary Stirring Type (AREA)
Abstract
The invention discloses a mixed fluid stirring mechanism and a tubular reactor, wherein a forward stirring structure and a reverse stirring structure are arranged on a main shaft, paddles of the forward stirring structure and paddles of the reverse stirring structure are spirally arranged on the main shaft, and the directions of acting forces generated by the forward stirring structure and paddles are opposite.
Description
Technical Field
The invention relates to a mixed fluid stirring mechanism and a tubular reactor.
Background
Stirring equipment is often used in the fields of chemical reaction, material preparation and the like, and the existing stirring equipment is basically a mechanical stirrer, and a stirring rod (or a stirring shaft) is driven to rotate by power equipment so as to enable paddles arranged on the stirring rod to move, so that stirring is realized. However, this mechanical stirring method has a certain problem.
First, when a mechanical stirrer on the market is applied to a tubular reactor for chemical reaction, raw materials of reactants need to enter from one end of the tubular reactor, after the chemical reaction occurs in a tube, the raw materials are output from the other end of the tubular reactor, so that the mechanical stirrer in the tubular reactor is required to have not only a stirring function, but also a function of conveying raw materials of the reactants from one end of the tubular reactor to the other end, and the conventional mechanical stirrer cannot meet the requirement of conveying materials in the tubular reactor.
In addition, the propeller blades or the sheet-form blades of the existing stirring equipment can generate stronger circumferential speed under the condition that the rotating shaft rotates at a high speed, so that incompatible stirring materials with different densities are separated under the action of centrifugal force, and the aim of mixing different materials is not achieved.
Disclosure of Invention
In order to solve the problems, the invention provides a mixed fluid stirring mechanism tubular reactor, which can obtain a stronger mixing effect under the condition of low energy consumption, can better solve the problem of conveying materials in the reactor, and makes up the technical situation that the conveying problem in the reactor cannot obtain a good effect.
In order to achieve the above purpose, the present invention adopts the following technical scheme:
the utility model provides a mixed fluid rabbling mechanism, includes the main shaft, be provided with forward stirring structure and reverse stirring structure on the main shaft, forward stirring structure and reverse stirring structure's paddle are laid on the main shaft spiral, and the effort direction of the production of both is opposite.
By the design, when the main shaft rotates, the forward stirring structure generates an axial upward driving force, and the reverse stirring structure generates an axial downward driving force, so that opposite-impact mixing is realized.
Of course, the stirring mechanism can also be used for stirring single materials.
Further, a convection area is reserved between the forward stirring structure and the reverse stirring structure, and the convection area part does not extend by the paddles.
Preferably, the axial length of the gaps between the stirring structures is 0.2 to 4 times the length of the stirring structures, so that the materials can be fully mixed.
Further, the blades of the forward stirring structure and the reverse stirring structure at the two sides of the convection area are spirally and alternately extended.
Further, the blades of the forward stirring structure and/or the reverse stirring structure are space spiral curved surfaces or spiral planes. So as to better drive the material to move along the axial direction.
Further, the tangential direction of the first end part of the spiral structure of the blade of the forward stirring structure and/or the reverse stirring structure is vertical or nearly vertical to the axial direction of the main shaft; the normal direction of the tangential plane of the second end part is perpendicular or nearly perpendicular to the axial direction of the main shaft.
Such a design ensures that during rotation of the spindle, fluid comes into contact with the first end of the helix and flows up (or down) the helix, the fluid velocity becoming vertical as the second end of the helix is reached.
Preferably, a vertical section is additionally arranged at the second end of the spiral structure so as to enhance the drainage capacity of the stirring structure in the vertical direction.
Preferably, the normal coaxial line direction of the tangential plane of the blade ends of the forward and reverse stirring structures near the convection region is perpendicular or nearly perpendicular.
The above-mentioned near vertical means that the angle from the vertical differs by not more than 15 °.
Further, the forward stirring structure and the reverse stirring structure are provided with 2-10 paddles along the circumferential direction of the main shaft.
The spiral structure of the forward stirring structure can give forward driving force to the stirring material in the axial direction when rotating, and the spiral structure of the reverse stirring structure can give backward driving force to the stirring material in the axial direction when rotating
Further, the driving force generated by the forward stirring structure is greater than the driving force generated by the reverse stirring structure. Or, the effective working area of the forward stirring structure is larger than that of the reverse stirring structure.
As an alternative embodiment, the number of paddles and the helix angle of the forward stirring structure and the reverse stirring structure are the same, and the area of the forward stirring structure is larger than that of the reverse stirring structure.
A preferred embodiment of this embodiment is:
the forward stirring structure and the reverse stirring structure have the same height, and the width of the forward stirring structure is larger than that of the reverse stirring structure, preferably 1.01 to 2 times of the width thereof.
Another preferred embodiment of this embodiment is:
the width of the forward stirring structure is the same as that of the reverse stirring structure, and the height of the forward stirring structure is greater than that of the reverse stirring structure;
Another preferred embodiment of this embodiment is:
The forward stirring structure and the reverse stirring structure are the same in height and length, and the blades of the reverse stirring structure are provided with a plurality of notches;
as a further preferable embodiment of this embodiment, there is provided:
the forward stirring structure and the reverse stirring structure are the same in height, and the pitch of the forward stirring structure is larger than that of the reverse stirring structure.
As another alternative embodiment, the helix angle and area of the forward and reverse stirring structures are the same, and the number of paddles of the forward stirring structure is greater than that of the reverse stirring structure.
As yet another alternative embodiment, the helix angle, the number of paddles, the height, the length, or/and the shape of the forward and reverse agitating structures are different.
One or more parameters of the spiral angle, the number of paddles, the height, the length and the shape of the forward stirring structure and the reverse stirring structure are different. The specific parameters are those which may be determined based on the specific stirring fluid and requirements.
Further, the main shaft is connected with a power device through a coupler.
A fluid agitator comprises the agitation mechanism.
The utility model provides a tubular reactor, includes the reactor body, this internal main shaft that is provided with of reactor is provided with the cavity in the main shaft, and the main shaft both ends are provided with the entry of heat transfer medium respectively, are provided with the import and the export of reactant on the reactor body, the main shaft outside is provided with forward stirring structure and reverse stirring structure, through the rotation of main shaft, forward stirring structure and reverse stirring structure produce axial thrust, realize the opposite dash mixing of the reactant in the reactor body.
Furthermore, a plurality of heat exchange chambers which are isolated from each other are arranged in the main shaft, and inlets are respectively arranged at two ends of the main shaft, so that the sectional temperature control in the reaction process can be realized through the design. Meanwhile, the upper chamber and the lower chamber can be filled with different heat exchange media, so that the heat exchange is performed in the reaction with high heat exchange rate, and the heat exchange effect is improved.
Furthermore, the inlets at the two ends of the main shaft are respectively provided with a rotary joint. The split inflow of the heat exchange medium is convenient, the sectional temperature control operation of the reactor is convenient to realize, the phenomenon that the temperature difference between the heat exchange medium at the inlet and the other end is overlarge is avoided, the speed of circulating liquid is reduced, and meanwhile, the heat exchange effect is improved.
Further, the inlets on the reactor body include at least two inlets for inputting different reactants, respectively.
Preferably, the reactant mass density input at the inlet located higher in the vertical direction is greater than the reactant mass density input at the inlet located lower. The design mode can enhance the mixing of materials under the action of gravity and buoyancy of different raw materials.
Preferably, the reactor can be vertical or horizontal, the vertical reactor can be vertically provided with a lower inlet and an upper outlet, so that the outlet position is higher than the inlet position, and the lower inlet and the upper outlet are also provided with the outlet position higher than the inlet position when the reactor is horizontally used, so that the reactants can be better mixed in an effective reactor mixing path under the influence of gravity.
Further, a sealing assembly is arranged at the connecting end part of the reactor body and the main shaft, so that leakage of reactants is prevented when the main shaft rotates, and sealing inside the tubular reactor shell is maintained.
Further, the main shaft penetrates through the sealing assemblies at the two ends, so that the inlet of the heat exchange medium is exposed outside the sealing assemblies.
Preferably, the width of the blades of the forward stirring structure and/or the reverse stirring structure is 0.2 times to 0.95 times the radial length of the annular space from the outside of the main shaft to the inner side of the shell of the reactor body.
Further, the inner diameters of the cavities may be uniform or non-uniform.
The working principle of the invention is as follows:
The main shaft has certain stirring effect in the high-speed rotation process, and the different arrangement forms of the blades with the forward and reverse foot plate structures connected with the main shaft can generate flow velocity from an inlet to an outlet in the rotation process of the main shaft, and the arrangement mode and the interval are adjusted according to different reaction conditions, so that the aim of conveying and stirring materials is finally achieved.
The stirring effect is achieved, a new heat exchange device is not needed, the heat exchange of reactants is carried out by utilizing the hollow cavity of the main shaft, and the reaction temperature is controlled inside the tubular reactor through a heat exchange medium, so that the effects of reducing side reactions and improving the reaction yield are achieved.
Compared with the prior art, the invention has the beneficial effects that:
1. According to the invention, through the staggered arrangement of the stirring structures connected with the main shaft, the aim of hedging and mixing is achieved, and meanwhile, the stirring materials can be driven to move upwards, so that the stirring materials can move in the axial direction from the inlet to the outlet;
2. The invention adopts a hedging mixing mode, avoids separation of stirring materials with different densities caused by centrifugal movement under the condition of overhigh rotating speed, and has better mixing effect when the rotating speed is higher;
3. According to the invention, the heat exchange upper chamber and the heat exchange lower chamber are separated for heat exchange, so that the effect of sectional temperature control in the pipeline can be realized, and heat exchange media with different characteristics are introduced according to the proceeding degree and the temperature requirement of different reactions;
4. The main shaft structure of the invention has small total volume, has strong applicability to the tubular reactor with limited space, and improves the space utilization rate inside the tubular reactor.
Drawings
The accompanying drawings, which are included to provide a further understanding of the application and are incorporated in and constitute a part of this specification, illustrate embodiments of the application and together with the description serve to explain the application.
FIG. 1 is a schematic diagram of a spindle configuration of the present invention;
FIG. 2 is a top view of the spindle configuration of the present invention;
FIG. 3 is a schematic view of a tubular reactor according to the present invention;
FIGS. 4 (a) -4 (c) are detailed views of stirring structures;
Fig. 5 is a schematic view of another embodiment of the spindle of the present invention.
Wherein: the device comprises a main shaft, a 2-heat exchange medium channel, a 3-heat exchange chamber, a 4-lower connecting pipe, a 5-upper connecting pipe, a 6-forward stirring structure, a 7-reverse stirring structure, an 8-rotary joint, a 9-heat exchange medium inlet, a 10-heat exchange medium outlet, an 11-coupler, a 12-tubular reactor shell, a 13-stirring material I inlet, a 14-stirring material II inlet, a 15-product outlet, a 16-exhaust port, a 17-power device, an 18-sealing component, a 19-stirring structure first end, a 20-stirring structure second end, a 21-stirring structure, an arrow direction is the main shaft rotating direction, and an A is a vertical section.
The specific embodiment is as follows:
the invention will be further described with reference to the drawings and examples.
It should be noted that the following detailed description is illustrative and is intended to provide further explanation of the application. Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this application belongs.
It is noted that the terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of exemplary embodiments according to the present application. As used herein, the singular is also intended to include the plural unless the context clearly indicates otherwise, and furthermore, it is to be understood that the terms "comprises" and/or "comprising" when used in this specification are taken to specify the presence of stated features, steps, operations, devices, components, and/or combinations thereof.
In the present invention, terms such as "upper", "lower", "left", "right", "front", "rear", "vertical", "horizontal", "side", "bottom", etc. refer to an orientation or a positional relationship based on that shown in the drawings, and are merely relational terms, which are used for convenience in describing structural relationships of various components or elements of the present invention, and do not denote any one of the components or elements of the present invention, and are not to be construed as limiting the present invention.
In the present invention, terms such as "fixedly attached," "connected," "coupled," and the like are to be construed broadly and refer to either a fixed connection or an integral or removable connection; can be directly connected or indirectly connected through an intermediate medium. The specific meaning of the terms in the present invention can be determined according to circumstances by a person skilled in the relevant art or the art, and is not to be construed as limiting the present invention.
As described in the background art, there are existing mechanical stirring devices in the prior art, and the substances often cause uneven mixing during the mixing or reaction process, so as to solve the above technical problems, the present application proposes a stirring device and a reactor.
In an exemplary embodiment of the present application, as shown in fig. 1, there is provided a stirring device including a main shaft 1, and a forward stirring structure 6 and a reverse stirring structure 7 provided on the main shaft 1.
The forward stirring structure 6 and the reverse stirring structure 7 spiral up on the main shaft 1, and when the main shaft 1 rotates due to the spiral direction of the forward stirring structure 6, the material is pushed to move upwards (or downwards) axially. The spiral direction of the reverse stirring structure 7 can enable the main shaft to rotate so as to push the material to move in the axial downward (or upward) direction.
Preferably, a convection area is reserved between the forward stirring structure 6 and the reverse stirring structure 7, and no paddle extends in the convection area. The axial length of the convection zone in the stirring structure is preferably 0.2 to 4 times that of the forward stirring structure 6 or the reverse stirring structure 7, so that the materials can be mixed in the convection zone for complete mixing.
The regions of the forward stirring structures 6 and the reverse stirring structures 7 on both sides of the convection region are non-convection regions, and the height of the regions of the non-convection regions can be zero or any height.
As an embodiment, the blades of the forward stirring structures 6 and the reverse stirring structures 7 on both sides of the convection region are spirally extended while being staggered. The paddles may or may not intersect, and may not be spatially staggered.
As shown in fig. 4 (a) -4 (b), the stirring structure 21 is preferably a space spiral curved surface structure, and may be a spiral plane structure. The stirring structure can enable the material to move towards the axial direction. A vertical section is added at the second end of the spiral structure to enhance the drainage capacity of the stirring structure in the vertical direction, as shown in fig. 4 (c).
Preferably, the two ends of the stirring structure 21 are provided with a tangential plane of the first end, and the angle between the tangential plane and the axial direction of the main shaft is greater than or equal to 60 degrees, preferably vertical or nearly vertical; the angle of the tangential plane of the second end in the normal coaxial line direction is less than or equal to 30 degrees, preferably the two are parallel or nearly parallel. When the main shaft rotates, the extending direction of the first end of the forward stirring structure 6 is basically the same as the rotating direction of the main shaft, or the crossing angle is smaller than 45 degrees, and the first end is close to the entering direction of the stirring material (the first end is close to the inlet of the stirring material if the reaction tube is a straight tube, the material enters the stirring area of the forward stirring structure 6 from the first end if the reaction tube is a bent tube), and the second end is close to the flowing direction of the stirring material (the second end is close to the inlet of the stirring material if the reaction tube is a straight tube, and the material enters the stirring area of the forward stirring structure 6 from the second end if the reaction tube is a bent tube). When the main shaft rotates, the extending direction of the first end of the reverse stirring structure 7 is basically the same as the rotating direction of the main shaft, or the crossing angle is smaller than 45 degrees, the first end is close to the outflow direction of the stirring material, and the second end is close to the inflow direction of the stirring material.
When the tangential direction of the first end is perpendicular or nearly perpendicular to the axial direction of the main shaft, the material can enter the stirring areas of the forward stirring structure 6 and the reverse stirring structure 7 better. When the normal coaxial line direction of the tangent plane of the second end is parallel or nearly parallel, the pushing force in the axial direction can not be applied to the materials basically, and the mixing of the materials can be better realized.
The spiral structure of the forward stirring structure 6 gives forward driving force to the stirring material in the axial direction when rotating, and the spiral structure of the reverse stirring structure 7 gives backward driving force to the stirring material in the axial direction when rotating.
The reactants, as a preferred embodiment, may be provided with a vertical section at the second end 20 of the stirring structure to enhance the ability of the stirring structure to drain in the vertical direction.
At the second end of the forward stirring structure 6 and the reverse stirring structure 7 near the convection zone.
By arranging different structures of the forward stirring structure 6 and the reverse stirring structure 7, the pushing force of the forward stirring structure 6 to the materials is larger than that of the reverse stirring structure 7.
To achieve the above effect, the modification of the stirring structure may include the following embodiments:
In the first embodiment, the area of the forward stirring structure 6 is larger than that of the reverse stirring structure 7 when the same spiral angle and the same number of blades are provided.
As a preferred example of the first embodiment, the forward stirring structure 6 and the reverse stirring structure 7 are the same in height, the width of the forward stirring structure 6 is larger than the width of the push-down stirring structure 7, and preferably the width of the forward stirring structure 6 is 1.01 to 2 times the width of the push-down stirring structure 7;
As another preferable example of the first embodiment, the forward stirring structure 6 and the reverse stirring structure 7 have the same width, and the height of the forward stirring structure 6 is larger than that of the reverse stirring structure 7;
As another preferable example of the first embodiment, the forward stirring structure 6 and the reverse stirring structure 7 have the same height and length, but the blades of the reverse stirring structure 7 are notched;
As still another preferable example of the first embodiment, the forward stirring structure 6 and the reverse stirring structure 7 have the same height, and the pitch of the forward stirring structure is larger than that of the reverse stirring structure.
In the second embodiment, the forward stirring structure 6 and the reverse stirring structure 7 have the same spiral angle and stirring structure area, and the number of the blades of the forward stirring structure 6 is greater than that of the reverse stirring structure 7, for example, the number of the blades of the forward stirring structure is 4, and the number of the reverse stirring structure is 3.
Of course, as other embodiments, the structural changes in the above preferred modes may be adopted simultaneously or in combination, as long as the capability of the forward stirring structure 6 to drive the material is greater than that of the reverse stirring structure 7.
As shown in fig. 2, both the forward stirring structures 6 and the reverse stirring structures 7 are uniformly and alternately distributed on the main shaft 1. As a preferable mode, the forward stirring structure 6 and the reverse stirring structure 7 are uniformly distributed and arranged for 2-10 pieces in the circumferential direction.
The number, helix angle, pitch, blade width, blade height, shape, size and/or number of the gaps of the forward stirring structure 6 and the reverse stirring structure 7 can be flexibly adjusted according to the type of the reactant of the stirring materials to be mixed and the required mixing (or reaction) intensity, and a plurality of the parameters can be selected to be changed.
As shown in fig. 3, a tubular reactor is provided, which comprises a main shaft 1, wherein a plurality of forward stirring structures 6 and reverse stirring structures 7 are arranged on the main shaft 1.
Preferably, the main shaft 1 includes a heat exchange chamber 3 therein, however, in other embodiments, the chamber may be split into a plurality of chambers, such as two chambers, specifically including an upper chamber and a lower chamber, where the upper chamber and the lower chamber are separated by a partition, and each of the upper chamber and the lower chamber has a respective inlet and a respective outlet.
The heat exchange medium flows in from an opening of the heat exchange cavity 3 connected with the main shaft, the heat exchange cavity 3 is provided with an opening at one end of the main shaft 1, the main shaft 1 is provided with an upper connecting pipe 5 and a lower connecting pipe 4 which are communicated with the heat exchange cavity 3, and the main shaft 1 is provided with a plurality of forward stirring structures 6 and reverse stirring structures 7.
The two ends of the main shaft are respectively provided with a rotary joint 8, the rotary joints are respectively connected with a heat exchange medium inlet 9 and a heat exchange medium outlet 10, the heat exchange medium inlet 9 is communicated with the heat exchange chamber 3, and the heat exchange medium outlet 10 is communicated with the heat exchange chamber 3; the upper end of the main shaft 1 is connected with a coupler 11; the coupling 11 is connected with a power device 17 to provide rotary power for the reactor. The heat exchange medium inlet 9 and the heat exchange medium outlet 10 can be exchanged according to practical situations, the inlet is changed into an outlet, and the outlet is changed into an inlet.
The tubular reactor shell 12 is internally provided with a mixed fluid stirring main shaft, the mixed fluid stirring main shaft is rotationally fixed at two ends of the tubular reactor shell 12, and the tubular reactor shell 12 and the mixed fluid stirring main shaft are sealed by adopting a sealing assembly 18.
The upper and lower parts of the tubular reactor shell 12 are provided with a stirring material I inlet 13 and a stirring material II inlet 14; the tubular reactor housing 12 is provided with both an outlet 15 for the mixed material and an exhaust port 16.
The structure of main shaft 1 can reduce the circumferencial direction velocity of movement of tubular reactor inside liquid in rotatory in-process, avoids the material separation that leads to because of the centrifugal force that circumferencial direction moved, and two kinds of stirring structures are crisscross to be set up simultaneously, can form powerful convection current well, improves the turbulence intensity and the mixing effect of the inside material of reactor.
The heat exchange medium inlet 9, the upper connecting pipe 5 and the heat exchange chamber 3 sequentially form a communicated channel, the heat exchange medium can flow in the channel formed by the heat exchange medium inlet, the heat exchange medium can flow in the forward direction or the reverse direction, and the heat exchange medium can flow in the forward direction or the reverse direction. Meanwhile, under the rotation condition of the main shaft 1, the forward stirring structure 6 and the reverse stirring structure 7 can form stable convection, and the reactants of the stirring materials are uniformly mixed. Meanwhile, when the stirring structure is designed, the forward pushing capacity of the forward stirring structure 6 is slightly larger than the reverse pushing capacity of the reverse stirring structure 7, so that the reaction requirement that the stirred material reactant can be stably conveyed forward is met.
When different stirred material reactants enter the tubular reactor shell 12 from the stirred material I inlet 13 and the stirred material II inlet 14 according to the reaction requirement, the stirred material II inlet 14 with relatively high position is generally filled with materials with relatively high density, the stirred material I inlet 13 with relatively low position is generally filled with materials with relatively low density, and the mixture of the materials of different types is enhanced under the action of gravity and buoyancy; the main shaft 1 is rotationally fixed at two ends of the tubular reactor shell 12, and the main shaft 1 rotates under the power action of the power device 17 to drive the forward stirring structure 6 and the reverse stirring structure 7 to move;
Wherein the width of the blades of the forward stirring structure 6 and the reverse stirring structure 7 is 0.2 to 0.95 times of the radial length from the outside of the main shaft 1 to the inside of the annular space of the tubular reactor shell 12;
The temperature in the reaction process is mainly completed by the cooperation of a heat exchange cavity 3, a lower connecting pipe 4, an upper connecting pipe 5, a heat exchange medium inlet 9 and a heat exchange medium outlet 10.
The rotary fixing place of the tubular reactor shell 12 and the main shaft 1 is provided with a sealing assembly 18, and the sealing assembly 18 is used for ensuring the sealing performance of the inside of the reactor shell under the condition that the main shaft 1 rotates or is static.
As an implementation mode, the heat exchange chamber 3 can be arranged in the middle of the main shaft, so that the sectional temperature control of the reaction can be realized, the reaction with high heat exchange is facilitated, the heat exchange is carried out, and the heat exchange effect is improved. The rotary joint 8 is divided into an upper rotary part and a lower rotary part which are respectively connected with the heat exchange medium inlet and the heat exchange medium outlet; the rotary joints 8 are sleeved at the two ends of the main shaft 1 in an inner side and an outer side.
Of course, as another implementation mode, a plurality of heat exchange chambers are arranged in the middle of the main shaft, so that the sectional temperature control of the reaction can be realized, and different heat exchange media can be introduced into the upper chamber and the lower chamber, thereby being beneficial to the high-heat exchange reaction for heat exchange and improving the heat exchange effect. The rotary joint 8 is divided into an upper rotary part and a lower rotary part, and is respectively connected with the lower heat exchange medium inlet and the upper heat exchange medium inlet, so that the heat exchange medium can flow in separately, and at the moment, each rotary joint can be provided with an independent outlet, so that the sectional temperature control operation of the reactor is conveniently realized, the phenomenon that the temperature of the heat exchange medium at the inlet is too high with the temperature difference at the other end part is avoided, the speed of circulating liquid is reduced, and the heat exchange effect is improved; the rotary joints 8 are sleeved at the two ends of the main shaft 1 in an inner side and an outer side; because the inlet of each heat exchange chamber is separated, the heat exchange chambers do not need to be subjected to excessive treatment, and the structural complexity of the rotary joint 8 is reduced, so that the processing difficulty and the production cost of the rotary joint are reduced.
Of course, as another embodiment, the inner diameter and/or the length of the heat exchange chamber are different, and can be adjusted according to the type, temperature, etc. of the heat exchange medium.
As another embodiment, the reactor may be used in a horizontal position or in an inclined position. The reaction time and the stirring and mixing time are adjusted and set according to the viscosity and other parameters of the reaction materials.
As another embodiment, a temperature regulating device is arranged outside the reactor.
The stirring part in the reactor improves the form and arrangement mode of the traditional paddles, the special paddle form can convert the rotating circumferential motion into the axial motion of the materials under the condition that the main shaft rotates at a high speed, and the up-down convection mixing form is formed by different arrangement modes, so that the circumferential motion strength in the reactor is greatly reduced, the mixing problem of stirring materials with different densities and mutually incompatibility is solved, and the applicability of the reactor is improved.
Meanwhile, a sectional temperature-control heat exchange structure is formed by arranging independent heat exchange chambers 3. Can obtain stronger mixing effect and heat exchange effect under the condition of low energy consumption, can better solve the problem of material transportation in the reactor, make up the technical current situation that the problem of transportation in the reactor can not obtain good effect.
The above description is only of the preferred embodiments of the present application and is not intended to limit the present application, but various modifications and variations can be made to the present application by those skilled in the art. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present application should be included in the protection scope of the present application.
While the foregoing description of the embodiments of the present invention has been presented in conjunction with the drawings, it should be understood that it is not intended to limit the scope of the invention, but rather, it is intended to cover all modifications or variations within the scope of the invention as defined by the claims of the present invention.
Claims (13)
1. A mixed fluid stirring mechanism, comprising a main shaft, characterized in that: the main shaft is provided with a forward stirring structure and a reverse stirring structure, the blades of the forward stirring structure and the reverse stirring structure are spirally arranged on the main shaft, and the directions of the generated acting forces are opposite;
A convection area is reserved between the forward stirring structure and the reverse stirring structure, and the convection area part does not extend with paddles;
The paddles of the forward stirring structure and the reverse stirring structure extend in a spiral and staggered manner;
The blades of the forward stirring structure and/or the reverse stirring structure are space spiral curved surfaces or spiral planes;
The direction of the tangential plane of the first ends of the forward stirring structure and the reverse stirring structure is the angle of more than or equal to 60 degrees with the axial direction of the main shaft; the angle of the tangential plane of the second end in the normal coaxial line direction is less than or equal to 30 degrees;
the spiral structure of the forward stirring structure can give forward driving force to the stirring material in the axial direction when rotating, and the spiral structure of the reverse stirring structure can give backward driving force to the stirring material in the axial direction when rotating;
the axial forward driving force of the rotation generated by the forward stirring structure is greater than the axial backward driving force generated by the reverse stirring structure;
the effective acting area of the forward stirring structure is larger than that of the reverse stirring structure.
2. A mixed fluid stirring mechanism as set forth in claim 1, wherein: the axial length of the gap between the stirring structures is 0.2 to 4 times of the length of the stirring structures, so that the materials can be fully mixed.
3. A mixed fluid stirring mechanism as set forth in claim 1, wherein: the tangential direction of the first ends of the forward stirring structure and the reverse stirring structure is perpendicular to the axial direction of the main shaft; the normal coaxial line direction of the tangential plane of the second end is parallel.
4. A mixed fluid stirring mechanism as set forth in claim 1, wherein: and a vertical section is additionally arranged at the second end of the spiral structure so as to enhance the drainage capacity of the stirring structure in the vertical direction.
5. A mixed fluid stirring mechanism as set forth in claim 1, wherein: the number of paddles and the spiral angle of the forward stirring structure and the reverse stirring structure are the same, and the effective acting area of the forward stirring structure is larger than that of the reverse stirring structure;
Or the heights of the forward stirring structure and the reverse stirring structure are the same, and the width of the forward stirring structure is larger than that of the reverse stirring structure;
or the width of the forward stirring structure is the same as that of the reverse stirring structure, and the height of the forward stirring structure is larger than that of the reverse stirring structure;
Or the forward stirring structure and the reverse stirring structure are the same in height and length, and the blades of the reverse stirring structure are provided with a plurality of notches;
or, the heights and the lengths of the forward stirring structures and the reverse stirring structures are the same, and the number of the forward stirring structures is larger than that of the reverse stirring structures.
6. A mixed fluid stirring mechanism as set forth in claim 5, wherein: the forward stirring structures and the reverse stirring structures are identical in height and length, the number of the forward stirring structures is greater than that of the reverse stirring structures, and the excessive forward stirring structures are uniformly distributed along the main shaft.
7. A mixed fluid stirring mechanism as set forth in claim 1, wherein: when the main shaft rotates, the extending direction of the first ends of the forward stirring structure and the reverse stirring structure is basically the same as the rotating direction of the main shaft, or the cross exists, and the cross angle is smaller than 45 degrees, but the directions of the first ends of the forward stirring structure and the reverse stirring structure are opposite.
8. A mixed fluid stirring mechanism as set forth in claim 1, wherein: one or more parameters of the spiral angle, the number of paddles, the height, the length and the shape of the forward stirring structure and the reverse stirring structure are different.
9. A fluid mixer comprising a mixing mechanism as claimed in any one of claims 1 to 8.
10. A tubular reactor, characterized by: the reactor comprises a reactor body, wherein the stirring mechanism as claimed in any one of claims 1-8 is arranged in the reactor body, the stirring mechanism comprises a main shaft, inlets of heat exchange media are respectively arranged at two ends of the main shaft, an inlet and an outlet of reactants are arranged on the reactor body, a forward stirring structure and a reverse stirring structure are arranged on the outer side of the main shaft, and axial pushing force is generated by the forward stirring structure and the reverse stirring structure through rotation of the main shaft, so that opposite-flushing mixing of the reactants in the reactor body is realized.
11. A tubular reactor as claimed in claim 10, wherein: a cavity is arranged in the main shaft.
12. A tubular reactor as claimed in claim 10, wherein: the density of the reactant materials input at the inlet with higher position in the vertical direction is larger than that of the reactant materials input at the inlet with lower position.
13. A tubular reactor as claimed in claim 10, wherein: the width of the blades of the forward stirring structure and/or the reverse stirring structure is 0.2 to 0.95 times of the radial length from the outside of the main shaft to the inner annular space of the shell of the reactor body.
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| CN201711471893.8A CN108554335B (en) | 2017-12-29 | 2017-12-29 | Mixed fluid stirring mechanism and tubular reactor |
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| CN201711471893.8A CN108554335B (en) | 2017-12-29 | 2017-12-29 | Mixed fluid stirring mechanism and tubular reactor |
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| CN111229105B (en) * | 2020-02-12 | 2022-04-05 | 淮南北新建材有限公司 | Mix quick-witted foaming homogenization system |
| CN111848438B (en) * | 2020-07-29 | 2023-05-23 | 浙江鼎龙科技股份有限公司 | Process for preparing 4, 6-diphenyl azo resorcinol and 4, 6-diamino resorcinol |
| CN112209793B (en) * | 2020-09-30 | 2022-04-08 | 广东石油化工学院 | Friedel-crafts alkylation reaction product and continuous synthesis method thereof |
| WO2024065073A1 (en) * | 2022-09-26 | 2024-04-04 | 深圳市华先医药科技有限公司 | Dynamic micro-channel tubular continuous flow reactor |
| CN115400623B (en) * | 2022-09-30 | 2024-01-30 | 广州天沅硅胶机械科技有限公司 | Sizing material mixes core and includes its mixing apparatus |
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