CN104907031A - Low-backmixing middle-speed reactor being capable of continuous feeding and operation method therefor - Google Patents
Low-backmixing middle-speed reactor being capable of continuous feeding and operation method therefor Download PDFInfo
- Publication number
- CN104907031A CN104907031A CN201510245413.0A CN201510245413A CN104907031A CN 104907031 A CN104907031 A CN 104907031A CN 201510245413 A CN201510245413 A CN 201510245413A CN 104907031 A CN104907031 A CN 104907031A
- Authority
- CN
- China
- Prior art keywords
- reactor
- central
- intermediate reactor
- reaction
- disk
- 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.)
- Pending
Links
Landscapes
- Physical Or Chemical Processes And Apparatus (AREA)
Abstract
The invention provides a low-backmixing middle-speed reactor being capable of continuous feeding. The middle-speed reactor is characterized in that the middle-speed reactor comprises a vertical and cylindrical reactor housing and a clamp cover at the outer side, a central stirring shaft, at least an A-shaped disc, at least a B-shaped disc, and a plurality of stirring paddles; a central annular gas is left between the center of the A-shaped disc and the central stirring shaft and used for flowing of a liquid; the center of the B-shaped disc and the central stirring shaft are fixedly connected, a peripheral annular gap is left between the periphery of the B-shaped disc and the inner wall of the reactor and used for flowing of a liquid; the plurality of stirring paddles are fixedly connected with the central stirring shaft; the A-shaped discs and the B-shaped discs are arranged on the central stirring shaft alternatively, and the reactor is divided into a plurality of reaction chambers in the axial direction; one stirring paddle is arranged in each reactor chamber. The low-backmixing middle-speed reactor can provide high-efficiency two-phase mixing and reaction stay time of some hours, and can lower backmixing degree greatly.
Description
Technical field
The present invention relates to a kind of can the intermediate reactor of low back-mixing of continuous feed, the invention still further relates to a kind of method of operating of intermediate reactor, belong to field of chemical equipment.
Background technology
There is a class in industrial reactor containing the heterogeneous reaction device of liquid phase, comprise solution-air, liquid-liquid, liquid-solid, gas-liquid-solid phase reactor.Its common feature to provide enough contacts area between phase and phase, realizes interphase mass transfer, chemical reaction could occur.Actual reaction speed is not only relevant with the speed of reaction itself, also relevant with mass transfer velocity.And mass transfer velocity is relevant with alternate contact area.In heterogeneous fast reaction, the effect of phase Contact and mass transfer may be even the key factor determining real reaction speed (macroreaction speed).
Comprise the heterogeneous reaction device of liquid phase, have the characteristic that some are common, the explanation of its mechanism can be example with liquid phase reaction.
Conventional liquid phase industrial reactor has the patterns such as packed tower, bubble tower, bubbling stirred tank, is mainly applicable to fast respectively, reacts with middling speed at a slow speed.Fast reaction can complete within a few second or a few minutes, and real reaction speed depends primarily on the contact area of gas-liquid two-phase; Slow reaction needs just can complete for more than several hours usually, and real reaction speed depends primarily on the volume of liquid phase; Middling speed reaction falls between, and needs contact area and the liquid phase volume of taking into account gas-liquid two-phase.So the gas liquid phase reactor being applicable to middling speed reaction needs to be smashed by bubble in liquid phase main body, to increase the surface area that unit volume bubble has usually.
Many organic heterogeneous reactions are consecutive reactions, and the product namely reacted can react further and generate other product.When intermediate product is required object product, just there is one " optimum reacting time ", the yield of object product is the highest at that time.Liquid phase reaction mass is made up of countless micelle, and the reaction time (time stopped in reactor) of each micelle experience is different, and the conversion ratio reached is also different.And the overall reaction effect of reactor is the comprehensive of these micelle differential responses effects.All to experience " optimum reacting time " effect best for each micelle in theory.In the reaction system of continuous-flow, the mixing between the fluid micellar of the different time of staying is called " back-mixing ", and the size of back-mixing degree uses " the zero dimension variance " of residence time destribution to characterize usually.The back-mixing of laminar flow is minimum, and its zero dimension variance is 0; The back-mixing of " complete mixing flow " of continuous-flow stirred tank is maximum, and its zero dimension variance is 1; The back-mixing degree of plural serial stage continuous stir reactor is close to laminar flow, and its zero dimension variance is less, reasonable in design can be less than 0.2 even 0.1.When being generally less than 0.2, low back-mixing can be referred to as.Generally speaking, low back-mixing is conducive to improving the reaction conversion ratio of consecutive reaction and selective.
Summary of the invention
The object of the present invention is to provide a kind of can the intermediate reactor of low back-mixing of continuous feed, efficient gas-liquid two-phase can either be provided to mix, increase gas-liquid contact surface area, can greatly reduce back-mixing degree again, make the overall flow state of reactor close to laminar flow.Simultaneously can provide the reaction time reaching a few hours, thus can reach higher conversion ratio and selective, meet the needs of liquid phase middling speed consecutive reaction preferably.
Present invention employs following technical scheme,
Can the intermediate reactor of low back-mixing of continuous feed, it is characterized in that, comprising: the shell of reactor of right circular cylinder shape; Central agitator axle, is arranged at the central authorities of intermediate reactor; Motor and gearbox, drive central agitator axle to rotate; At least one A type disk, leaves central annular space between its central authorities and central agitator axle, flows through for liquid; At least one Type B disk, its central authorities are fixedly connected with central agitator axle, leave periphery annular space, flow through for liquid between periphery and the inwall of intermediate reactor; And multiple paddle, be fixedly connected with central agitator axle, A type disk and Type B disk are disposed alternately on central agitator axle, and intermediate reactor is separated into multiple reative cell vertically, and paddle is distributed among each reative cell.
In addition, of the present invention can the intermediate reactor of low back-mixing of continuous feed, can also have such feature: wherein, the ratio of height to diameter of shell of reactor is 2 ~ 10.
In addition, of the present invention can the intermediate reactor of low back-mixing of continuous feed, can also have such feature: wherein, the arranged outside heat exchange jacket of intermediate reactor, flows through for heat exchanging fluid, with the reaction mass heat exchange in intermediate reactor.
In addition, of the present invention can the intermediate reactor of low back-mixing of continuous feed, such feature can also be had: shell of reactor has at least one tower joint, between tower joint, use ring flange to be connected.
In addition, of the present invention can the intermediate reactor of low back-mixing of continuous feed, can also have such feature: wherein, the periphery of A type disk coordinates for dynamic with between reaction tower inwall, dynamic cooperation place has flexible sealing material, and when disk rotational, liquid barrier material flows through.
In addition, of the present invention can the intermediate reactor of low back-mixing of continuous feed, can also have such feature: wherein, the bottom of shell of reactor and the side at top have feed inlet and outlet.
The present invention also provides a kind of method of operating of intermediate reactor, it is characterized in that, comprises the following steps:
Step one, the reaction mass be pre-mixed is injected the first reative cell, motor and gearbox drive central agitator axle to rotate, and then drive paddle stirring reaction material to make it even, pulverize the bubble in reaction mass;
Step 2, reaction mass flow to follow-up reative cell successively from the first reative cell, and reative cell is separated intermediate reactor inside by adjacent A type disk and Type B disk and formed,
Leave central annular space between the central authorities of A type disk and central agitator axle, flow through for liquid;
Its central authorities of Type B disk are fixedly connected with central agitator axle, leave periphery annular space, flow through for liquid between periphery and the inwall of intermediate reactor,
Reaction mass when flowing through each reative cell alternately through central annular space and periphery annular space;
Step 3, when the time that reaction mass stops in intermediate reactor arrives the optimum reacting time of this reaction, product is discharged from discharging opening.
In addition, the method for operating of intermediate reactor of the present invention, can also have such feature: wherein, in step one and step 2, while carrying out reacting, carries out heat exchange between reaction mass and heat exchanging fluid.
The beneficial effect of the invention
Of the present invention can the intermediate reactor of low back-mixing of continuous feed, efficient gas-liquid two-phase can either be provided to mix, increase alternate contact surface area, improve the speed of heterogeneous reaction; Can greatly reduce back-mixing degree again, make the overall flow state of intermediate reactor close to laminar flow, be conducive to improving the selective of consecutive reaction; And the reaction mass stop reaction time in the reactor can be made to reach a few hours, improve the conversion ratio of middling speed reaction.Thus the needs of liquid phase middling speed consecutive reaction can be met preferably.
Accompanying drawing explanation
Fig. 1 be of the present invention can the internal structure schematic diagram of intermediate reactor of low back-mixing of continuous feed.
Detailed description of the invention
Below in conjunction with accompanying drawing, the specific embodiment of the present invention is described.
As shown in Figure 1, of the present invention can the intermediate reactor of low back-mixing of continuous feed, comprise shell of reactor 11; Central agitator axle 14; Motor 10, gearbox 214; Multiple A type disk 15; Multiple Type B disk 16; Paddle 17; And multiple reative cell.
Shell of reactor 11, comprises two Jie Tajie in the present embodiment, and in using between tower joint, ring flange 212 is connected, and is convenient to carry out Precision Machining to tower body.Also have upper flange plate 213 on the top of shell of reactor 11, there is the mechanical seal of central agitator axle 14 at upper flange plate 213 center, has four supports by edge, for placing motor 10 and gearbox 214.The bottom of shell of reactor 11 has lower flange 211.The axle sleeve of location is inserted in the lower end of central agitator axle 14, and axle sleeve fixed radial is connected to the central authorities of lower flange 211.The ratio of height to diameter of shell of reactor is 2 ~ 10.The bright and clean rounding of inwall of intermediate reactor.The arranged outside heat exchange jacket 12 of intermediate reactor, heat exchanging fluid flows through heat exchange jacket 12, with the reaction mass heat exchange in intermediate reactor.The upper end of shell of reactor 11 is a flat head, and central authorities are sealing ring; Lower end is ellipse head.
Central agitator axle 14, is arranged at the central authorities of intermediate reactor, rotates under the drive of motor 10 and gearbox 214.
Motor 10 and gearbox 214, be arranged on the top of shell of reactor 11, drives central agitator axle 14 to rotate.
A type disk 15, leaves annular space between its central authorities and central agitator axle 14, is called central annular space 151.From then on reactant liquor flows through in central annular space 151, thus enters in adjacent reative cell.The periphery of A type disk 15 coordinates for dynamic with between shell of reactor 11 inwall, and cooperation place has rubber and plastic flexible material, and when disk rotational, liquid barrier material flows through.
Type B disk 16, is fixedly connected on central agitator axle 14, leaves annular space between the inwall of periphery and shell of reactor 11, be called periphery annular space 161.From then on reactant liquor flows through in periphery annular space 161.
A type disk 15 and Type B disk 16 are disposed alternately on central agitator axle 14, and the interior separation of intermediate reactor is become multiple reative cell.In present embodiment, the quantity of reative cell has six, is respectively the first reative cell 131, second reative cell 132, the 3rd reative cell 133, the 4th reative cell 134, the 5th reative cell 135 and the 6th reative cell 136 from the bottom to top.
All there is among each reative cell a paddle 17, central agitator axle 14 has multiple paddle 17, Stirring under the drive of motor 10 and gearbox 214, the form of paddle 17 can be turbine type, propeller type or the special blade be set directly on A type dish and Type B dish.
The lower end of shell of reactor 11 is also provided with tangential feed inlet and outlet 18, vertical feed inlet and outlet 19; Its upper end arranges feed inlet and outlet 20.In the present embodiment, owing to adopting the mode of lower endfeed upper end discharging, therefore, tangential feed inlet and outlet 18 and/or vertical feed inlet and outlet 19 are used as charging aperture, and upper end feed inlet and outlet 20 is used as discharging opening.
Can the running of intermediate reactor of low back-mixing of continuous feed:
Being entered by tangential admission mouth 18 through the gas phase that mixes instantaneously and liquid phase reacting material can the intermediate reactor of low back-mixing of continuous feed, first be stirred in the first reative cell 131 of foot, in whipping process, bubble is pulverized, and liquid phase contact surface area increases, and reacts.Be assumed to be exothermic reaction, reaction heat passes by the cooling medium in heat exchange jacket.
Because reactant mixture constantly flows into from bottom, after the first reative cell 131 initial reaction, constantly upwards flow into the second reative cell 132 with same flow.In the second reative cell 132, continuing gassing pulverizing---liquid phase reaction---, the processes such as jacket heat transfer, the conversion ratio of reaction mass improves further.Then the like, until reactant liquor leaves last reative cell at intermediate reactor top, i.e. the 6th reative cell 136.Now reaction mass can continuous feed low back-mixing intermediate reactor in stop reaction time arrive near optimum value, product is flowed out by discharging opening 20.
Because fluid alternately passes through central annular space 151 and periphery annular space 161, add being uniformly mixed and efficient mass transfer/reaction in each reative cell.Between adjacent reaction room, fluid is on the whole in one-way flow, so intermediate reactor of the present invention can provide very large gas liquid film to amass, effectively promotes the mass transfer between gas-liquid two-phase and reaction, fast reaction speed, shortens the time required for reaction.Residence time destribution is close to laminar flow simultaneously, and back-mixing degree is low, is conducive to the yield improving consecutive reaction object product.The volume of intermediate reactor can be enough large, a large amount of liquid phase reacting materials can be held, thus can under the mode of operation of fluid continuous-flow, meet the reaction time reaching less than several hours, make middling speed reaction can experience the relatively long reaction time and reach the conversion ratio of expection.
Certainly, due to the general character that heterogeneous reaction has, except for except the liquid phase reaction in above-described embodiment, of the present invention can the intermediate reactor of low back-mixing of continuous feed for liquid-liquid, liquid-solid, gas-liquid-solid reaction system, can be suitable for too.
Claims (8)
1. can the intermediate reactor of low back-mixing of continuous feed, it is characterized in that, comprising:
The shell of reactor of right circular cylinder shape;
Central agitator axle, is arranged at the central authorities of described intermediate reactor;
Motor and gearbox, drive described central agitator axle to rotate;
At least one A type disk, leaves central annular space between its central authorities and described central agitator axle, flows through for liquid;
At least one Type B disk, its central authorities are fixedly connected with described central agitator axle, leave periphery annular space, flow through for liquid between the inwall of periphery and described intermediate reactor; And
Multiple paddle, is fixedly connected with described central agitator axle,
Described A type disk and described Type B disk are disposed alternately on described central agitator axle, and described intermediate reactor is separated into multiple reative cell vertically,
Described paddle is distributed among each described reative cell.
2. according to claim 1 can the intermediate reactor of low back-mixing of continuous feed, it is characterized in that:
Wherein, the ratio of height to diameter of described shell of reactor is 2 ~ 10.
3. according to claim 1 can the intermediate reactor of low back-mixing of continuous feed, it is characterized in that:
Wherein, the arranged outside heat exchange jacket of described intermediate reactor, flows through for heat exchanging fluid, with the reaction mass heat exchange in described intermediate reactor.
4. according to claim 1 can the intermediate reactor of low back-mixing of continuous feed, it is characterized in that:
Described shell of reactor has at least one tower joint, uses ring flange to be connected between described tower joint.
5. according to claim 1 can the intermediate reactor of low back-mixing of continuous feed, it is characterized in that:
Wherein, coordinate for dynamic between the periphery of described A type disk and the inwall of described intermediate reactor, dynamic cooperation place has flexible sealing material, and when disk rotational, liquid barrier material flows through.
6. according to claim 1 can the intermediate reactor of low back-mixing of continuous feed, it is characterized in that:
Wherein, the bottom of described shell of reactor and the side at top have feed inlet and outlet.
7. a method of operating for intermediate reactor, is characterized in that, comprises the following steps:
Step one, the reaction mass be pre-mixed is injected the first reative cell, motor and gearbox drive central agitator axle to rotate, and then drive paddle stirring reaction material to make it even, pulverize the bubble in reaction mass;
Step 2, reaction mass flow to follow-up reative cell successively from the first reative cell, and described reative cell is separated described intermediate reactor inside by adjacent A type disk and Type B disk and formed,
Leave central annular space between the central authorities of described A type disk and described central agitator axle, flow through for liquid;
Its central authorities of described Type B disk are fixedly connected with described central agitator axle, leave periphery annular space, flow through for liquid between the inwall of periphery and described intermediate reactor,
Reaction mass when flowing through each reative cell alternately through central annular space and periphery annular space;
Step 3, when the time that reaction mass stops in described intermediate reactor arrives the optimum reacting time of this reaction, product is discharged from discharging opening.
8. the method for operating of intermediate reactor according to claim 7, is characterized in that:
Wherein, in described step one and step 2, while carrying out reacting, between reaction mass and heat exchanging fluid, heat exchange is carried out.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510245413.0A CN104907031A (en) | 2015-05-14 | 2015-05-14 | Low-backmixing middle-speed reactor being capable of continuous feeding and operation method therefor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510245413.0A CN104907031A (en) | 2015-05-14 | 2015-05-14 | Low-backmixing middle-speed reactor being capable of continuous feeding and operation method therefor |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN104907031A true CN104907031A (en) | 2015-09-16 |
Family
ID=54076715
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510245413.0A Pending CN104907031A (en) | 2015-05-14 | 2015-05-14 | Low-backmixing middle-speed reactor being capable of continuous feeding and operation method therefor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104907031A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108014732A (en) * | 2016-10-28 | 2018-05-11 | 中国石油化工股份有限公司 | A kind of aging method of continuous ageing reactor and aluminium hydroxide |
| CN113398868A (en) * | 2021-07-16 | 2021-09-17 | 浙江工业大学 | Tower type continuous flow reactor and application thereof |
| CN113499749A (en) * | 2021-07-20 | 2021-10-15 | 浙江工业大学 | Method and device for continuously preparing biodiesel by multiple towers in series connection |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4442273A (en) * | 1983-04-06 | 1984-04-10 | Atlantic Richfield Company | Process and apparatus for continuous polymerization of a monovinyl aromatic monomer |
| EP0434124A1 (en) * | 1989-12-15 | 1991-06-26 | Shell Internationale Researchmaatschappij B.V. | Multistage reactor |
| US20010031226A1 (en) * | 1996-03-13 | 2001-10-18 | Esa Korhonen | Apparatus for the polymerization of olefin monomers |
| CN1694916A (en) * | 2002-09-23 | 2005-11-09 | 通用电气公司 | Continuous manufacture of silicone copolymers via multi-stage blade-mixed plug flow tubular reactor |
| US20100093931A1 (en) * | 2008-07-24 | 2010-04-15 | Lanxess Inc. | Process for the continuous hydrogenation of carbon-carbon double bonds in an unsaturated polymer to produce a hydrogenated polymer |
| CN102658050A (en) * | 2012-05-16 | 2012-09-12 | 浙江长城减速机有限公司 | Multi-stage continuous curing tank for hydrophobically associating polymer |
-
2015
- 2015-05-14 CN CN201510245413.0A patent/CN104907031A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4442273A (en) * | 1983-04-06 | 1984-04-10 | Atlantic Richfield Company | Process and apparatus for continuous polymerization of a monovinyl aromatic monomer |
| EP0434124A1 (en) * | 1989-12-15 | 1991-06-26 | Shell Internationale Researchmaatschappij B.V. | Multistage reactor |
| US20010031226A1 (en) * | 1996-03-13 | 2001-10-18 | Esa Korhonen | Apparatus for the polymerization of olefin monomers |
| CN1694916A (en) * | 2002-09-23 | 2005-11-09 | 通用电气公司 | Continuous manufacture of silicone copolymers via multi-stage blade-mixed plug flow tubular reactor |
| US20100093931A1 (en) * | 2008-07-24 | 2010-04-15 | Lanxess Inc. | Process for the continuous hydrogenation of carbon-carbon double bonds in an unsaturated polymer to produce a hydrogenated polymer |
| CN102658050A (en) * | 2012-05-16 | 2012-09-12 | 浙江长城减速机有限公司 | Multi-stage continuous curing tank for hydrophobically associating polymer |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108014732A (en) * | 2016-10-28 | 2018-05-11 | 中国石油化工股份有限公司 | A kind of aging method of continuous ageing reactor and aluminium hydroxide |
| CN108014732B (en) * | 2016-10-28 | 2023-11-21 | 中国石油化工股份有限公司 | Continuous aging reactor and aging method of aluminum hydroxide |
| CN113398868A (en) * | 2021-07-16 | 2021-09-17 | 浙江工业大学 | Tower type continuous flow reactor and application thereof |
| CN113499749A (en) * | 2021-07-20 | 2021-10-15 | 浙江工业大学 | Method and device for continuously preparing biodiesel by multiple towers in series connection |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101444715B (en) | Self-suction mixing reactor | |
| CN100584445C (en) | Stirring/flow-guiding multi-phase reactor | |
| CN201046396Y (en) | Non-rotary vertical cyclic liquid knockout reactor | |
| CN201366323Y (en) | High-efficiency stirring device | |
| CN110193333B (en) | Gas-liquid-solid multiphase tubular stirring reactor | |
| CN104907031A (en) | Low-backmixing middle-speed reactor being capable of continuous feeding and operation method therefor | |
| CN201300057Y (en) | Self-priming stirred reactor | |
| CN201394451Y (en) | Novel polymeric kettle | |
| CN100577277C (en) | Self-suction type inner circulation overweight field gas-liquid reactor | |
| CN205386443U (en) | But reation kettle stirring rake of independent assortment | |
| CN101708382A (en) | Extraction and back-extraction device | |
| US4378436A (en) | Process and device for improving the quality of mixing of liquid especially viscous media | |
| CN101549261A (en) | Improved-blade type disc turbine stirring device | |
| CN104437310B (en) | A kind of reactor with cooling device | |
| CN2636982Y (en) | Synthesis reaction kettle | |
| CN103769028A (en) | Novel reaction apparatus | |
| CN101745292B (en) | Multilevel open type turbine rotary disc agitated column for ketene continuous absorption and application thereof | |
| CN104209070A (en) | Internal circulation type hydrogenation reaction kettle | |
| CN114247412A (en) | Chemical production uses high-efficient type reation kettle | |
| CN200960413Y (en) | Effective constitution of plants separating laboratory modular assembly device | |
| CN211754926U (en) | Reaction device for multistage accelerated reaction | |
| CN102133517A (en) | Liquid continuous impact flow heterogeneous reaction and aerobic fermentation technical equipment | |
| CN206325567U (en) | A kind of esterifying kettle of improved structure | |
| CN202238056U (en) | Organic carbonic ester reaction kettle and stirring device thereof | |
| CN201593047U (en) | Liquid continuous impinging stream multi-phase reaction and aerobic fermentation technical equipment |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C02 | Deemed withdrawal of patent application after publication (patent law 2001) | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20150916 |