CN205627930U - Extrinsic cycle formula alkylation reaction ware - Google Patents
Extrinsic cycle formula alkylation reaction ware Download PDFInfo
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- CN205627930U CN205627930U CN201620231727.5U CN201620231727U CN205627930U CN 205627930 U CN205627930 U CN 205627930U CN 201620231727 U CN201620231727 U CN 201620231727U CN 205627930 U CN205627930 U CN 205627930U
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Abstract
The utility model relates to an extrinsic cycle formula alkylation reaction ware. The utility model discloses an extrinsic cycle formula alkylation reaction ware is including emulgator and heat exchanger, the emulgator include: the emulgator casing, stirring motor, (mixing) shaft, axial -flow type paddle, footpath STREAMING paddle, baffle, component distributor, inlet pipe and discharge gate, the heat exchanger include: heat exchanger shell, heat exchange array pipe, heat transferring medium import, heat exchange medium outlet, matter entrance, material export and result export, the emulgator is connected through first connecting pipe and second connecting pipe with the heat exchanger. The emulgator can realize the low suitable dispersed emulsion and suitably accuse temperature who glues the material of low -density in the high density resisting medium, the axial -flow type paddle that the heat exchanger has been strengthened in the reaction accuse wen bingyu emulgator drives the material circulation in coordination, has guaranteed that the dispersed emulsion mass transfer among the alkylation reaction, reaction move nice and warm fluid circulation the flow stability and the adjustable of three kinds of functions.
Description
Technical field
This utility model belongs to field of chemical equipment, more specifically, this utility model relates to a kind of outer circulation
Formula alkylation reactor.
Background technology
Alkylated reaction refers to that the hydrogen atom being connected in organic compound molecule on carbon, oxygen and nitrogen is by alkyl institute
Substituted reaction.A kind of typical alkylated reaction is butane and butylene life under the catalytic action of concentrated sulphuric acid
Become the alkylated reaction of isobutyltrimethylmethane..In the reaction of this sulfuric acid alkylation, butylene is dissolved in concentrated sulphuric acid as reaction
The continuous phase of system, the butane being not easy concentrated sulphuric acid is then dispersion phase, and butane is anti-with the alkylation of butylene
Should occur on two-phase interface.In order to improve reaction efficiency, need to strengthen its mass transfer area, and by alkane
Being effectively dispersed in concentrated sulphuric acid continuous phase is one of important channel strengthening its mass transfer.But because of product isobutyltrimethylmethane.
And isomerization product dissolubility in concentrated sulfuric acid is the most relatively low accordingly, and for improving the conversion ratio of alkene
Have employed high alkane alkene ratio and have a large amount of unreacted alkane, therefore alkane and product be required for as early as possible with urge
Agent concentrated sulphuric acid separates, to improve production efficiency.This just require alkane dispersion and emulsion in concentrated sulfuric acid without
Homogenize, but the most controlled.Meanwhile, sulphuric acid catalysis butane is strong with the alkylated reaction of butylene
Exothermic reaction, system needs to control cryogenic conditions, and the viscosity of the concentrated sulphuric acid under low temperature is higher, therefore
This emulsifying is the dispersive process in the resisting medium containing thermal transmission requirement.
Patent CN204107349U discloses a kind of novel silicon oil emulsion reactor, installs in reactor
Anchor oar, coil pipe and high-shear emulsion machine, reduced silicon oil viscosity by heating, added in high-speed emulsifying machine
Add more blade and improve the measures such as rotating speed to improve product emulsifying uniformity.Patent
CN204685014U discloses a kind of high-shear emulsifying device, internal multilamellar after being heated by device chuck
Zigzag disk high speed shear effect carrys out fortified milk quality.Patent 201410184576.8 discloses one
Emulsion mixing device, coordinates promotion flowing mixing up and down to improve effect by what multiaxis frame stirred with leaf formula
Really.Patent CN201603524U discloses a kind of emulsifier unit, uses and is provided with the paddle of through hole to thing
Material is circulated emulsifying to improve emulsifying effectiveness.Patent 204447838U discloses a kind of silicone oil emulsification dress
Put, use electromagnetic excitation to drive the rotating vane on disk to achieve the uniform stirring that dynamics is gentle.Patent
202446992U provides a kind of silicone oil emulsification agitating device, real with the teeter column between co-axially fixed disk
Show the emulsion process that mixing force is less.Patent 102961987A provides a kind of company with premixing
The high viscous silicone oil emulsification technique of continuousization and equipment thereof, have employed comprise premixing screw pump, static mixer,
The equipment such as emulsifying stirred tank obtain high viscous silicone oil emulsification product, use difference in its emulsifying stirred tank
The oblique leaf oar of blade quantity.Patent CN204247083U provides a kind of emulsifier unit, in emulsion tank
Mulser rotating shaft on be provided with two and counter push away wheel, emulsifying capacity can be effectively improved, make emulsifying more thorough
Finer and smoother.Patent CN204582987U provides a kind of mulser, is provided with on multiple on shaft
The agitator arm of lower stacking coordinates with stator, is sent out by sidepiece supersonic generator and bottom ultrasound wave simultaneously
Raw device makes medium can carry out ultrasonic emulsification on the basis of machinery emulsification, and the media diameters after emulsifying is more
Little, emulsifying effectiveness is more preferably.In above-mentioned patent, target product is the product emulsion of long-time stable, does not has
Product split-phase separation requirement, and without chemical reaction, be not suitable as there is chemical reaction, applied catalysis
The reaction system of agent, the dispersion and emulsion of alkylation reaction system of such as sulfuric acid catalysis.
Patent CN104667856A, CN104549086A, CN104549115A, CN104549108A,
CN104549116A、CN104549111A、CN104549110A、CN104549109A、
CN104549087A, CN104549114A etc. arrange injection hybrid component and at reactor in reactor
Interior installation revolving bed or inside and outside revolving bed, to realize the dispersion mixing of catalyst and reactant.This kind of reaction
Device realizes the assembly of reaction system dispersion and emulsion too much, complexity is installed, be not easy to the high efficiency manufacture of equipment.
Patent CN200520078557.3 discloses a kind of horizontal alkylation reactor, and employing propeller will
Dispersion, mixing are incorporated into synchronization implementation in same equipment with heat exchange, but to immiscible liquid-liquid reactions system
Shearing dispersion, mixing and fluid interchange ability consider insufficient.
Patent CN103242895A discloses a kind of carbon 4 alkylation production method and device, liquid phase C4
Alkane and concentrated sulphuric acid utilize agitating device fully emulsified outside device, complete alkane in multistage tower reactor
Glycosylation reaction.This patented method ensure that the emulsifying degree of the sour hydrocarbon entering reactor, but reacted in tower
The interface of the emulsion in journey updates depends on filler, and its in good time regulation measure is few.
Patent CN203764234U discloses a kind of alkylation reactor, and its reactor includes top
Material inlet and distributed rendering section, the conversion zone at middle part and the product segregation section of bottom.Material distribution is mixed
Conjunction section reaches material in the case of without agitator by multi-pipeline distributor and is uniformly distributed mixing；In reaction
Section, equipped with filler, promotes the carrying out of reaction with mass transfer enhancement effect.It is real that this reactor can move heat by gasification
The most directly cool down.Being provided with too much material inlet pipeline in the material mixing section of this reactor, it is arranged
Complexity, flow resistance are big, are unfavorable for manufacturing, producing and safeguard.
Patent CN102921368B discloses a kind of Horizontal internal circulating stirred reactor, circulates with Strong shear
The compound action of stream blade, width gradual change baffle plate etc. realizes the dispersion of material and circulates.This reactor
In material dispersion emulsifying and circulate power and provided by same blade, be unfavorable for the regulation and control of emulsifying requirement,
Also it is unfavorable for the optimization of mass-and heat-transfer simultaneously.
To sum up, this area also needs to exploitation can increase mass transfer area, improve reaction efficiency alkylated reaction
Equipment.
Summary of the invention
The purpose of this utility model is to provide a kind of outer circulation type alkylation reactor and alkylated reaction side
Method.
In first aspect of the present utility model, it is provided that a kind of outer circulation type alkylation reactor, described reaction
Device includes emulsator and heat exchanger；Described emulsator includes: emulsator housing 3；Stirring drives motor 1；
Shaft 2, it is driven by stirring driving motor 1；Axial-flow type blade 201, it is positioned on shaft 2；
Radial-flow type blade 202, it is positioned on shaft 2；Baffle plate 4；Component distributor 6；Feed pipe 8；With
Discharging opening 10；Described heat exchanger includes: heat exchanger shell 13；Heat exchanging pipe 18；Heat transferring medium enters
Mouth 16；Heat transferring medium outlet 17；Material inlet 12；Material outlet 20；Product exit 14；Described
Reactor also includes the first connecting tube 11 and the second connecting tube 21 between emulsator and heat exchanger.
In a preference, described emulsator also includes: heat exchange jacket 5, it is positioned on housing exterior walls；
It is preferred that this heat exchange jacket 5 includes half tubular heat exchange coil.
In another preference, described emulsator also includes: material discharging hole 7.
In another preference, the pipe of half described tubular heat exchange coil built with flowing liquid phase or can phase
Become the liquid phase heat transferring medium of vaporization.
In another preference, described material discharging hole (7) also can be as charging aperture.
In another preference, described emulsator housing 3 includes: big housing 304；Small shell 302,
Its diameter is less than big housing 304；Transitional shell 303, it is used for connecting small shell 302 and big housing 304；
Little end socket 301, it is used for closing small shell 302 upper end；Big end socket 305, it is used for closing big housing
304 lower ends.
In another preference, the length of straight flange of described big housing 304 is described small shell 302
1～2 times of length of straight flange；Preferably 1.2～1.8 times；And/or the diameter of described big housing 304
For described shell of small shell diameter 1～3 times；Preferably 1.5～2.5 times.
In another preference, described discharging opening 10 is positioned at the sidewall of small shell 302.
In another preference, described feed pipe 8 is positioned on big housing 304 or big end socket 305.
In another preference, described component distributor 6 enters in big housing 304 through housing 3.
In another preference, described heat exchange jacket 5 is covered on the sidewall of big housing 304.
In another preference, described shaft 2 is through little end socket 301, at described big housing 304
Or be positioned in described big end socket 305.
In another preference, described transitional shell 303, big end socket 305 or little end socket 301 use
Elliposoidal end enclosure structure.
In another preference, described feed pipe 8 is additionally provided with recycle feed mouth 9.
In another preference, described feed pipe 8 passes perpendicularly through described big end socket 305；It is preferred that
The outlet of described feed pipe 8 is between described component distributor 6 and big end socket 305；More preferably,
The outlet of described feed pipe 8 is described feed pipe 8 apart from the vertical dimension of described component distributor 6
1～20 times of diameter；It is more preferably 2～10 times.
In another preference, described axial-flow type blade 201 is selected from: propeller, Aerofoil impeller；Preferably
Ground is propeller.
In another preference, within described axial-flow type blade 201 is positioned at small shell 302；It is preferred that
0.90～0.98 times (preferably 0.94～0.96 of a diameter of small shell 302 diameter of axial-flow type blade 201
Times)；And/or described axial-flow type blade 201 is installed on distance discharging opening 10 vertical dimension on shaft 2
Position for 0.8～1.5 times (preferably 0.9～1.4 times) of small shell 302 diameter.
In another preference, described radial-flow type blade 202 is selected from: straight leaf disc vane wheel oar, symmetrical
Recessed leaf disc vane wheel oar, asymmetric recessed leaf disc vane wheel oar, oblique leaf oar；Preferably disk vane wheel oar.
In another preference, within described radial-flow type blade 202 is positioned at big housing 304；It is preferred that
0.45～0.55 times (preferably 0.47～0.54 of a diameter of big housing 304 diameter of radial-flow type blade 202
Times)；And/or described radial-flow type blade 202 is installed on shaft 2 bottom the big end socket of distance 305
Vertical dimension is the position of 0.25～0.50 (preferably 0.3～0.4 times) of big housing 304 diameter.
In another preference, the quantity of described baffle plate 4 is 2～12；Preferably 2-10 sheet；
It is preferred that multi-piece baffle plate 4 is equally distributed.
In another preference, the width of described baffle plate 4 be the diameter of described big housing 304 1/20～
1/8；Preferably 1/12～1/10.
In another preference, the length of described baffle plate 4 is identical with the length of straight flange of big housing 304.
In another preference, the inwall of described baffle plate 4 and big housing 304 from span from for baffle plate
The 1/12～1/8 of 4 width.
In another preference, described component distributor 6 includes charging aperture 601 and distributor pipe 602；
It is distributed porose on described distributor pipe 602；It is preferred that described component distributor 6 is distributed for tubular type
Device；It is preferred that the ring diameter of described distributor pipe 602 is described radial-flow type blade 202 diameter 0.8～
1.2 again；It is more preferably 0.9～1.1 times.
In another preference, on distributor pipe 602, the aperture in the hole of distribution is 2～20mm.
In another preference, described component distributor 6 is installed on described radial-flow type blade 202 with big
Between end socket 305；It is preferred that between described component distributor 6 and described radial-flow type blade 202
Vertical dimension is 0.5～1.5 times of described radial-flow type blade 202 height, preferably 0.8～1.2 times.
In another preference, the top and bottom of described heat exchanger shell 13 are closed by end socket 15；
It is preferred that described heat transferring medium import 16 and heat transferring medium outlet 17 are present on end socket 15.
In another preference, also include in described heat exchanger: tubulation gripper shoe 19, change for fixing
Hot tubulation 18.
Other side of the present utility model is due to this disclosure, to those skilled in the art
It is apparent from.
Accompanying drawing explanation
Fig. 1, a kind of outer circulation type alkylation reactor structural representation of the present utility model be (positive apparent direction
Profile).In figure, dotted arrow represents that liquid stream flows to.
Fig. 2, the schematic diagram (vertical view direction) of tubular type component distributor.
The structural representation that Fig. 3, shaft position in emulsator, heat exchanging pipe positions in heat exchanger is (just
The profile of apparent direction).
Fig. 4, several radial-flow type paddle blade structure schematic diagram.It is followed successively by from left to right: straight leaf disc vane wheel oar,
Symmetrical recessed leaf disc vane wheel oar, oblique leaf oar.
Fig. 5, several Axial-flow impeller impeller structure schematic diagram.Upper left for arc propeller, upper in be fan-shaped spiral shell
Rotation oar, upper right is four leaf Aerofoil impeller, and bottom left is six wide leaf Aerofoil impeller, lower in be six narrow leaf Aerofoil impeller, under
The right side is k5 Aerofoil impeller.
In figure, each reference is respectively as follows:
1: stirring drives motor；
2: shaft；201: axial-flow type blade；202: radial-flow type blade；
3: emulsator housing；301: little end socket；302: small shell；303: transitional shell；304:
Big housing；305: big end socket.
4: baffle plate；
5: heat exchange jacket；
6: component distributor；601: charging aperture；602: distributor pipe；
7: material discharging hole (or feed pipe)；
8: feed pipe；
9: recycle feed mouth；
10: discharging opening；
11: the first connecting tubes；
12: material inlet；
13: heat exchanger shell；
14: product exit；
15: end socket；
16: heat transferring medium import；
17: heat transferring medium exports；
18: heat exchanging pipe；
19: tubulation gripper shoe；
20: material outlet；
21: the second connecting tubes.
Detailed description of the invention
In order to overcome the deficiency of prior art, the present inventor, through in-depth study, develops and follows outside one
Ring type alkylation reactor and alkylation reaction method.By mechanical agitation type Continuous Emulsifier and heat exchanger
Constituting material outside circulation, emulsator ensure that realizing the low viscous hydro carbons of low-density in high density resisting medium has
The suitable dispersion and emulsion of machine thing and suitable temperature control；Heat exchanger then enhance reaction temperature control and with in emulsator
Axial-flow type blade coordinated drive Matter Transfer, it is ensured that the dispersion and emulsion mass transfer in alkylated reaction, reaction
Move heat and the stability of three kinds of functions of circular fluidic flow and Modulatory character.
Term
As used herein, described " the low viscous material of low-density " refers to that a class has relatively low-density, relatively
Low viscous material；Such as, its density is typically 0.15～1g/cm3, its viscosity is typically 0.2～100CP.
Described " the low viscous material of low-density " is as dispersion phase.
As used herein, described " high density viscous material " refers to that a class has higher density, higher
The material of viscosity；Such as, its density is typically 1～5g/cm3Or its viscosity is typically 1～1000CP.
Described " high density viscous material " conduct " continuous phase ".
Should be understood that " the low viscous material of low-density " and " high density viscous material " are a kind of relative general
Reading, such as, if the viscosity of continuous phase is in the middle of 1～100CP (such as 20CP), the viscosity of dispersion phase is being less than
1CP (such as 0.5CP), then continuous phase is " high density viscous material " relative to dispersion phase.
Outer circulation type alkylation reactor
This utility model provides a kind of outer circulation type alkylation reactor, and described reactor includes emulsator
And heat exchanger, both are connected by connecting tube, carry out substance circulating.
Emulsator described in the utility model includes: emulsator housing, stirring driving motor, shaft,
Axial-flow type blade, radial-flow type blade, baffle plate, component distributor, feed pipe, discharging opening.
Described emulsator housing includes: big housing；Small shell；Transitional shell；Little end socket；Big end socket.
The diameter of described small shell is less than big housing.Described transitional shell is used for connecting small shell and big housing,
Described little end socket is used for closing small shell upper end, and described big end socket is used for closing big housing lower end, from
And integrant emulsator housing.As optimal way of the present utility model, described transitional shell,
Big end socket or little end socket use elliposoidal end enclosure structure.As optimal way of the present utility model, described
1～2 times of the length of straight flange that length of straight flange is described small shell of big housing；Preferably 1.2～1.8
Times.As optimal way of the present utility model, a diameter of described shell of small shell diameter of described big housing
1～3 times；Preferably 1.5～2.5 times.Should be understood that the situation according to reaction, big housing is with little
The height ratio of housing and diameter proportion also can be outside this range.
Described stirring drives motor to provide power for the operating for shaft, has suitable driving energy
The motor of power all can be applicable in this utility model.Described shaft passes little end socket, described big
It is positioned in housing or described big end socket.Generally, the agent structure of described emulsator housing is cylinder
The bodily form, and described shaft is located on the centrage of emulsator housing.
Described axial-flow type blade is installed on shaft, within being positioned at small shell.As this utility model
Optimal way, 0.90～0.98 times of a diameter of shell of small shell diameter of described axial-flow type blade；Preferably
0.94～0.96 times.As optimal way of the present utility model, described axial-flow type blade is installed on stirring
On axle, distance discharging opening vertical dimension is 0.8～1.5 times of shell of small shell diameter, preferably 0.9～1.4 times
Position.Described axial-flow type blade can be but not limited to: propeller or Aerofoil impeller；Preferably spiral shell
Rotation oar.Fig. 5 presents some axial-flow type blades
Described radial-flow type blade is installed on shaft, within being positioned at big housing.As this utility model
Optimal way, 0.45～0.55 times of a diameter of big diameter of the housing of described radial-flow type blade, preferably
0.47～0.54 times.As optimal way of the present utility model, described radial-flow type blade is installed on stirring
On axle vertical dimension is big diameter of the housing 0.25～0.50 times of the big end socket of distance, preferably 0.3～
The position of 0.4 times.Described radial-flow type blade can be but not limited to: straight leaf disc vane wheel oar, symmetrical
Recessed leaf disc vane wheel oar, asymmetric recessed leaf disc vane wheel oar or tiltedly leaf oar；Preferably disk vane wheel oar.
Fig. 4 presents some radial-flow type blades.
In order to coordinate radial-flow type blade, in big housing, also set up baffle plate near the position of medial wall, thus with
Radial-flow type blade acts on jointly, is disperseed by dispersion phase circulation shear and enters in continuous phase.The quantity of baffle plate
It it is at least 2；Generally 2～12；Preferably 2-10 sheet；Be more preferably 2-8 sheet, as 4,
6.Usually, in multi-piece baffle plate is uniformly arranged in big housing, the wall near medial wall is all.As this reality
With novel optimal way, the inwall of described baffle plate and big housing from span from for barrier width
1/12～1/8.As optimal way of the present utility model, the width of described baffle plate is described big housing
The 1/20～1/8 of diameter；Preferably 1/12～1/10.As optimal way of the present utility model, described
The length of baffle plate identical with the length of straight flange of big housing；Or
Described emulsator also includes heat exchange jacket, and it is positioned on emulsator housing exterior walls, and it can be used for adjusting
The temperature of the liquid in whole emulsator housing.Described heat exchange jacket can be arranged at big housing and small shell
On, or can be only arranged on big housing.As optimal way of the present utility model, described heat exchange is pressed from both sides
Set include half tubular heat exchange coil, its pipe built with flowing liquid phase or can phase transformation vaporization liquid phase heat exchange be situated between
Matter.
Described emulsator also includes component distributor, and it is arranged in big housing, it include charging aperture and
Distributor pipe, described distributor pipe is distributed porose.As optimal way of the present utility model, on distributor pipe
The aperture in the hole of distribution can be 2～20mm.As optimal way of the present utility model, described component
Distributor is tubular type distributor.It is preferred that the ring diameter of the distributor pipe of described component distributor is institute
0.8～1.2 times of the radial-flow type diameter of propeller blade stated；It is more preferably 0.9～1.1 times.As this utility model
Optimal way, described component distributor is installed between described radial-flow type blade and big end socket；Preferably
Ground, the vertical dimension between described component distributor and described radial-flow type blade is described radial-flow type blade
0.5～1.5 times of height, preferably 0.8～1.2 times.
Described emulsator also includes at least one feed pipe (charging aperture), at least one discharge nozzle (discharging
Mouthful).
Described feed pipe is positioned on big housing or big end socket；It is preferably located at big end socket bottom.As this
The optimal way of utility model, described feed pipe passes perpendicularly through described big end socket；Enter described in it is preferred that
It is additionally provided with recycle feed mouth on material pipe；Divide it is preferred that the outlet of described feed pipe is positioned at described component
Between cloth device and big end socket；More preferably, vertical apart from described distributor of outlet of described feed pipe
1～20 times of the diameter that distance is described feed pipe, is more preferably 2～10 times.
Described discharge nozzle is positioned on small shell, and it is for exporting emulsification product.
Described emulsator also includes material discharging hole, and it is positioned at the bottom of emulsator housing, for by breast
Changing after terminating, in emulsator, remaining material is discharged.Described material discharging hole also can be as charging aperture.
Heat exchanger described in the utility model includes: heat exchanger shell, heat exchanging pipe, heat transferring medium import,
Heat transferring medium exports, material inlet, material outlet, product exit.
The top and bottom of described heat exchanger shell are closed by end socket；It is preferred that described heat transferring medium
Import and heat transferring medium outlet are present on end socket.
Described heat exchanging pipe can be fixed in heat exchanger by tubulation support；It is preferred that heat exchanging pipe quilt
Fix equably.The gap of heat exchanging pipe allows Flow of Goods and Materials, thus with material generation heat exchange.
In described heat exchanger, heat transferring medium can be liquid phase or can phase transformation vaporization liquid phase heat transferring medium,
This heat transferring medium is entered described heat exchange row by the heat transferring medium import of described heat exchanger after end socket is distributed
In the pipe of pipe, and after the material-heat-exchanging between the pipe of the described heat exchanging pipe of described heat exchanger, change from described
The heat transferring medium outlet of hot device is flowed out.
The exchange capability of heat of described heat exchanger to meet the heat transfer requirements of alkylation reactor reaction temperature control is
Standard, and design effective heat exchange area and heat transferring medium condition accordingly.
Reactor described in the utility model also include the first connecting tube between emulsator and heat exchanger and
Second connecting tube, thus reaction mass can be carried between emulsator and heat exchanger.Described first
Connecting tube and the diameter of the second connecting tube, can determine according to the scale of emulsator and heat exchanger.
The application of outer circulation type alkylation reactor
This utility model additionally provides the purposes of described outer circulation type alkylation reactor, described outer follows
Ring type alkylation reactor is used for being alkylated reaction.
Described outer circulation type alkylation of the present utility model includes: the outer circulation type alkane described in offer
Glycosylation reaction device, inputs the first reaction mass by feed pipe in big housing；By component distributor to
Input the second reaction mass in big housing；Opening stirring and drive motor, the second reaction mass is at radial-flow type oar
Lower circulation shear is dispersed in the first reaction mass leaf with the common effect of baffle plate, then by small shell
After the further dispersion and emulsion of axial-flow type blade, the first reaction mass and the second reaction mass occur a part anti-
Ying Hou, the material of mixing is flowed out emulsator by discharging opening, is input to via the first connecting tube and material inlet
In heat exchanger.In heat exchanger, under suitable heat transfer boundary condition, the material of mixing continues to react, and by
Second connecting tube enters feed pipe, is flowed in emulsator, enters after mixing with the first fresh reaction mass
Row successive reaction；Reaction mass obtains target product from product exit output after subsequent operation.
When described emulsator is run, stirring drives the rotating speed of motor typically in the range of 100～800rpm
It is suitable.Certainly, according to kind and the difference of volume of material to be emulsified, the rotating speed of stirring is permissible
Being adjusted to the numerical value beyond above-mentioned scope, this is that those skilled in the art are prone to accomplish.
Described heat exchanger includes that heat transferring medium, described heat transferring medium are liquid phases or can phase transformation vaporize
Liquid phase heat transferring medium, this heat transferring medium is entered the pipe of heat exchanging pipe after end socket is distributed by heat transferring medium import
In, and after the material-heat-exchanging between the pipe of heat exchanger tube, flow out from heat transferring medium outlet.
Method of the present utility model is be applicable to carrying out the low viscous material of low-density high density viscous material
Dispersion and emulsion, and make two kinds of materials that sufficiently reaction occur.Method of the present utility model is particularly suitable
In the alkylated reaction needing high-viscosity material to participate in.
" alkylated reaction " described in the utility model refer to organic compound molecule is connected in carbon, oxygen and
The reaction that hydrogen atom on nitrogen is replaced by alkyl.Participate in reaction material the most immiscible and
Course of reaction occurs thermal change, it is therefore desirable to carry out dispersion and emulsion to promote that first is anti-by emulsator
Answer contacting with each other of thing and the second reactant, regulate suitable temperature by heat exchanger.
As optimal way of the present utility model, described " the first reaction mass " is as continuous phase
Material.Such as, concentrated sulphuric acid, its in alkylated reaction frequently as catalyst.More specifically as containing alkene
The concentrated sulphuric acid of hydrocarbon (preferably C3～C5 alkene, such as butylene).
As optimal way of the present utility model, described " the second reaction mass " is as dispersion phase
Material.Such as, hydro carbons；Preferably alkane；It is more preferably C3～C5 alkane, such as butane.
The input volume flow ratio of the first reaction mass and the second reaction mass input emulsator can be: even
Continuous phase: dispersion phase=1:1～10:1.Certainly, according to the needs of reaction, in some cases, other ratio
Example scope is also possible.
As a kind of embodiment, reactor of the present utility model is applicable to divide with concentrated sulphuric acid for continuous phase
Dissipate hydro carbons.Reactor of the present utility model, by regulation emulsator in the version of blade, diameter with
And speed of agitator regulates the blade shearing dispersibility to dispersion phase, it is thus achieved that suitable dispersion and emulsion drop
Diameter, when needing stable before dispersion and emulsion system split-phase in the liquid-drop diameter of this dispersion phase and subsequent process
Between corresponding.Meanwhile, sulphuric acid catalysis butane is strong exothermal reaction with the alkylated reaction of butylene, system
Needing to control cryogenic conditions, and the viscosity of the concentrated sulphuric acid under low temperature is higher, therefore this emulsifying is to comprise
Dispersive process in the resisting medium of thermal transmission requirement；Described emulsator can also be come by heat exchange jacket
Realize the regulation and control of temperature.Further, by the application of heat exchanger, perfect temperature is provided for reaction system
Adjusting ambient.
Major advantage of the present utility model is:
(1) emulsator use radial-flow type blade match with the baffle plate of installation, it is achieved efficient to material
Shear the emulsifying degree disperseing and reaching suitable.
(2) while dispersion and emulsion, it is achieved that the efficient renewal of reaction interface, mass transfer effect is enhanced,
Be conducive to improving reaction efficiency.
(3) in emulsator, the axial-flow type blade driving reaction system to flow it is provided with, it is simple to meet alkyl
Change the inside and outside ratio of the Matter Transfer needed for reaction.
(4) the reasonable setting of stirrer paddle rotating speed in emulsator, is conducive to regulating and controlling emulsifying effectiveness so that it is both
Reaction mass transfer area requirements can be met, product and excess alkane can be made again to be separated efficiently, improve raw
Produce efficiency.
(5) outside in circulation heat exchanger the part phase separation of material to produce severe poor, this severe difference with
Axial-flow type blade can produce synergism, the Matter Transfer function in enhanced reactor.
(6) outer circulation type heat exchanger makes heat exchange function have independence, it is possible to meet the regulation of enhanced heat transfer
Property and controllability, provide convenience for plant maintenance simultaneously.
Below in conjunction with specific embodiment, this utility model is expanded on further.Only should be understood that these embodiments
For this utility model being described rather than limiting scope of the present utility model.In the following example unreceipted
The experimental technique of actual conditions, generally according to normal condition, or according to the condition proposed by manufacturer.
Embodiment 1, outer circulation type alkylation reactor
1, mechanical agitation type Continuous Emulsifier
Such as Fig. 1 and Fig. 3, mechanical agitation type Continuous Emulsifier includes: emulsator housing 3；Emulsator shell
Body 3 includes: big housing 304；Small shell 302, its diameter is less than big housing 304；Transitional shell 303,
It connects small shell 302 and big housing 304；Little end socket 301, it closes small shell 302 upper end；Big end socket
305, it closes big housing 304 lower end.Described transitional shell 303, big end socket 305, little end socket 301
Use elliposoidal end enclosure structure.The 1.5 of the length of straight flange that length of straight flange is small shell 302 of big housing 304
Times.2 times of a diameter of shell of small shell diameter of big housing 304.
Also setting up heat exchange jacket 5 on the outer wall of big housing 304, this heat exchange jacket 5 includes half tubular heat exchange
Coil pipe, pipe built with flowing liquid phase or can phase transformation vaporization liquid phase heat transferring medium.
Shaft 2 is through little end socket 301, in described big housing 304 or described big end socket 305
Being positioned, shaft 2 is driven motor 1 to drive by stirring.
On shaft 2, axial-flow type blade 201 and radial-flow type blade 202 are set.
Axial-flow type blade 201 is positioned in small shell 302, uses propeller, and it is installed on shaft 2
Distance discharging opening 10 vertical dimension is the position of 1 times of small shell 302 diameter, its a diameter of small shell
0.95 times of 302 diameters.
Radial-flow type blade 202 is positioned at big housing 304, uses disc turbine oar, and it is installed on shaft
The position of bottom the big end socket of distance 305 0.35 times that vertical dimension is big housing 304 diameter on 2, its
0.5 times of a diameter of big housing 304 diameter.
Including component distributor 6 in big housing 304, it enters into big housing 304 through emulsator housing wall
In.Component distributor 6 is tubular type distributor, such as Fig. 2, including charging aperture 601 and distributor pipe 602；
It is distributed porose on distributor pipe 602；The diameter of distributor pipe 602 is the 0.95 of the diameter of radial-flow type blade 202
Times.On distributor pipe 602, the aperture in the hole of distribution is 5mm.Component distributor 6 is installed on described radial-flow type
Between blade 202 and big end socket 305, hanging down between component distributor 6 and described radial-flow type blade 202
Straight distance is 0.95 times of described radial-flow type blade 202 height.
Arranging baffle plate 4 in big housing 304, baffle plate 4 is uniformly arranged in the close inwall of big housing 304
Position, from span from for the 1/10 of baffle plate 4 width, the quantity of installation is 6.The length of baffle plate 4 with
The length of straight flange of big housing 304 is identical, and width is the 1/11 of the diameter of big housing 304.
Multiple material gateway is also set up, including feed pipe 8, discharging opening 10, thing on emulsator housing 3
Material discharging hole 7.Recycle feed mouth 9 it is additionally provided with on feed pipe 8.Discharging opening 10 is positioned at small shell 302
Sidewall.Feed pipe 8 is positioned on big end socket 305, and it passes perpendicularly through big end socket 305 and enters emulsator housing
Internal.The feed pipe 8 material outlet in emulsator housing is positioned at component distributor 6 and big end socket 305
Between, 6 times of the diameter that vertical dimension is feed pipe 8 of the distributor pipe 602 of distance component distributor 6.
2, heat exchanger
Heat exchanger includes: heat exchanger shell 13；Heat exchanging pipe 18；Heat transferring medium import 16；Heat exchange is situated between
Matter outlet 17；Material inlet 12；Material outlet 20；Product exit 14.Described heat exchanger shell 13
Top and bottom closed by end socket 15.Described heat transferring medium import 16 and heat transferring medium outlet 17
It is present on end socket 15.
Also include in described heat exchanger: tubulation gripper shoe 19, be used for fixing heat exchanging pipe 18.Comprise
In the end socket 15 of heat transferring medium import 16, it is additionally provided with the device of distribution heat transferring medium so that changing of inflow
Thermal medium is evenly distributed in heat exchanging pipe.
3, connecting tube
Described reactor also includes that the first connecting tube 11 and second between emulsator with heat exchanger is connected
Pipe 21, for carrying out the mass transfer between emulsator and heat exchanger.
Embodiment 2, outer circulation type alkylation
1, reactions steps
With simulation medium, (as continuous phase, isobutyltrimethylmethane. is dispersion phase to syrup saline solution.Continuous phase and dispersion phase
Density be 80:1 than the ratio of viscosities for 1.5:1, continuous phase and dispersion phase).Stirring at rotating speed 500rpm
Drive.
Utilizing the outer circulation type alkylation reactor described in embodiment 1 to be simulated reaction, step is as follows:
In the outer circulation type alkylation reactor described in embodiment 1, by feed pipe 8 in housing 3
Input continuous phase material (the first reaction mass), treats continuous phase material submergence radial-flow type blade 202 continuously
After, open stirring and drive motor 1；Then the most defeated in big housing 304 by component distributor 6
Enter dispersion phase material (the second reaction mass).
Dispersion phase material circulation shear under radial-flow type blade 202 with the common effect of baffle plate 4 is dispersed into
In continuous phase material, then by after the further dispersion and emulsion of axial-flow type blade 201 in small shell 302, warp
Discharging opening 10 flows out emulsator.Dispersion phase is being disperseed breast by radial-flow type blade 202 and axial-flow type blade 201
(this example have employed simulation medium simulation emulsifying, does not produce heat release for change and conveying；When being alkylated reaction,
Release reaction heat) simultaneously.The emulsion of partial reaction is there is through first even from what discharging opening 10 flowed continually out
Adapter 11 is entered between the pipe of the heat exchanging pipe 18 in heat exchanger 13 (when producing reaction heat by material inlet 12
Time, material during flow further downstream along between pipe with the medium generation heat exchange in heat exchanging pipe bundle 18 pipe
Effect, in the range of removing reaction liberated heat thus reaction temperature being maintained at suitably).Through heat exchange
Material after tubulation from the material outlet 20 of heat exchanger after the second connecting tube 21 merges with new material from entering
Material pipe 8 returns to emulsifying and reaction further in emulsator, and material is recycle stream between emulsator and heat exchanger
Dynamic.
From the material of emulsator inflow heat exchanger, can flow out from product exit 14 part and obtain through subsequent operation
Obtain target product.
2, reaction effect
The shifting thermic load of alkylation reactor is determined by process conditions, and the completeest by emulsator and heat exchanger
Become.The heat exchange efficiency of emulsator and heat exchanger and emulsator and the heat exchange area of heat exchanger and heat transferring medium
Turnover state parameter relevant with flowing velocity, simultaneously and also and emulsator in material and heat exchanger tube between thing
The flowing velocity of material is relevant.The heat exchange area of emulsator and heat exchanger is big, material and the flowing of heat transferring medium
The fast then heat exchange efficiency of speed is high, and heat transferring medium occurs vaporization phase transformation that heat exchange efficiency then can be made to significantly improve.
When design suitably reduces flow velocity in heat exchanger, material will occur phase separation.Dispersion phase because of
Density is low and floats and flows out from product exit, and continuous phase then settles because density is big.The sedimentation of continuous phase
Gravity is consistent with the conveying power upwards of the axial-flow type blade in emulsator, thus beneficially material is in emulsifying
Circulating between device and heat exchanger, promotes mass transfer, reaction and heat exchange.
The parameters such as the emulsifying degree of system material, emulsion droplet size, Matter Transfer flowing velocity reflect
The mass transfer of reaction and heat-transfer effect, these effects can be embodied in unresponsive simulation medium.
Use the method in aforementioned " 1 " to carry out Characterization result, from emulsator, gather emulsion carry out
The investigation of parameter, result is as follows:
(1) reaction mass emulsifying degree is investigated
Obtain the emulsion through emulsator emulsifying, investigate the time used by emulsion split-phase 50%.After measured,
The time needed during emulsion split-phase 50% is 40～65min.
Visible, in mechanical agitation type Continuous Emulsifier of the present utility model, use power input capability strong
Radial-flow type blade, matches with the baffle plate installed, adds the mating reaction of axial-flow type blade, it is achieved that right
The efficient of material shears the emulsifying degree disperseing and reaching suitable.
(2) reaction efficiency is investigated
Obtain the emulsion through emulsator emulsifying, investigate the liquid-drop diameter of dispersion phase.After measured, dispersion phase
Liquid-drop diameter d32The content of ＜ 80 μm is more than 80%.Dispersed phase drop diameter is little, is conducive to improving biography
Matter interfacial area and renewal thereof, thus improve reaction efficiency.
(3) Matter Transfer parameter is investigated
In course of reaction, measure reaction mass loop parameter.After measured, in terms of axial-flow type diameter of propeller blade
The circular flow number calculated is more than 0.71.Higher circular flow number is conducive to meeting the circulation of alkylated reaction
Inside and outside ratio, improves heat exchange efficiency.
(4) the unit volume power of agitator of dispersion and emulsion system consumes
After measured, the specific volume power consumption of dispersion and emulsion system is 3～10kw/m3In the range of.Can
Seeing, outer circulation type alkylation reactor of the present utility model has the highest production efficiency.
It should be noted that embodiment of the present utility model is only in order to illustrate technical side of the present utility model
Case and unrestricted.After having read above-mentioned teachings of the present utility model, those skilled in the art can
To make various changes or modifications this utility model, these equivalent form of values fall within right appended by the application equally
Claim limited range.
Claims (29)
1. an outer circulation type alkylation reactor, it is characterised in that described reactor includes emulsator and heat exchanger；
Described emulsator includes: emulsator housing (3)；Stirring drives motor (1)；Shaft (2), it is driven by stirring driving motor (1)；Axial-flow type blade (201), it is positioned on shaft (2)；Radial-flow type blade (202), it is positioned on shaft (2)；Baffle plate (4)；Component distributor (6)；Feed pipe (8) and discharging opening (10)；
Described heat exchanger includes: heat exchanger shell (13)；Heat exchanging pipe (18)；Heat transferring medium import (16)；Heat transferring medium outlet (17)；Material inlet (12)；Material outlet (20) and product exit (14)；
Described reactor also includes the first connecting tube (11) between emulsator and heat exchanger and the second connecting tube (21).
2. outer circulation type alkylation reactor as claimed in claim 1, it is characterised in that described emulsator also includes:
Heat exchange jacket (5), it is positioned on housing exterior walls；And/or
Material discharging hole (7).
3. outer circulation type alkylation reactor as claimed in claim 2, it is characterised in that this heat exchange jacket (5) includes half tubular heat exchange coil.
4. outer circulation type alkylation reactor as claimed in claim 1, it is characterised in that described emulsator housing (3) including:
Big housing (304)；
Small shell (302), its diameter is less than big housing (304)；
Transitional shell (303), it is used for connecting small shell (302) and big housing (304)；
Little end socket (301), it is used for closing small shell (302) upper end；
Big end socket (305), it is used for closing big housing (304) lower end.
5. outer circulation type alkylation reactor as claimed in claim 4, it is characterised in that
The length of straight flange of described big housing (304) is 1～2 times of the length of straight flange of described small shell (302)；And/or
1～3 times of a diameter of described shell of small shell diameter of described big housing (304).
6. outer circulation type alkylation reactor as claimed in claim 5, it is characterised in that the length of straight flange of described big housing (304) is 1.2～1.8 times of the length of straight flange of described small shell (302).
7. outer circulation type alkylation reactor as claimed in claim 5, it is characterised in that 1.5～2.5 times of a diameter of described shell of small shell diameter of described big housing (304).
8. the outer circulation type alkylation reactor as described in claim 1-2,4-5 are arbitrary, it is characterised in that
Described discharging opening (10) is positioned at the sidewall of small shell (302)；Or
Described feed pipe (8) is positioned on big housing (304) or big end socket (305)；Or
In described component distributor (6) enters into big housing (304) through housing (3)；Or
Described shaft (2) passes little end socket (301), is positioned in described big housing (304) or described big end socket (305)；Or
Recycle feed mouth (9) it is additionally provided with on described feed pipe (8)；Or
Described feed pipe (8) passes perpendicularly through described big end socket (305).
9. outer circulation type alkylation reactor as claimed in claim 8, it is characterised in that the outlet of described feed pipe (8) is positioned between described component distributor (6) and big end socket (305).
10. outer circulation type alkylation reactor as claimed in claim 9, it is characterized in that, 1～20 times that exports the diameter that vertical dimension is described feed pipe (8) apart from described component distributor (6) of described feed pipe (8).
11. outer circulation type alkylation reactors as claimed in claim 4, it is characterised in that described transitional shell (303), big end socket (305) or little end socket (301) use elliposoidal end enclosure structure.
12. outer circulation type alkylation reactors as claimed in claim 2, it is characterised in that described heat exchange jacket (5) is covered on the sidewall of big housing (304).
The 13. outer circulation type alkylation reactors as described in claim 1-5 is arbitrary, it is characterised in that described axial-flow type blade (201) is selected from: propeller, Aerofoil impeller；And/or
Within described axial-flow type blade (201) is positioned at small shell (302)；And/or
Described axial-flow type blade (201) is installed on the position of 0.8～1.5 times that upper distance discharging opening (10) vertical dimension of shaft (2) is small shell (302) diameter.
14. outer circulation type alkylation reactors as claimed in claim 13, it is characterised in that described axial-flow type blade (201) is propeller.
15. outer circulation type alkylation reactors as claimed in claim 13, it is characterised in that 0.90～0.98 times of a diameter of small shell (302) diameter of described axial-flow type blade (201).
The 16. outer circulation type alkylation reactors as described in claim 1-5 is arbitrary, it is characterised in that described radial-flow type blade (202) is selected from: straight leaf disc vane wheel oar, symmetrical recessed leaf disc vane wheel oar, asymmetric recessed leaf disc vane wheel oar, oblique leaf oar；And/or
Within described radial-flow type blade (202) is positioned at big housing (304)；And/or
Described radial-flow type blade (202) is installed on the position of vertical dimension is big housing (304) diameter 0.25～the 0.50 of shaft (2) the upper big end socket of distance (305) bottom.
17. outer circulation type alkylation reactors as claimed in claim 16, it is characterised in that described radial-flow type blade (202) is disc turbine oar.
18. outer circulation type alkylation reactors as claimed in claim 16, it is characterised in that 0.45～0.55 times of a diameter of big housing (304) diameter of described radial-flow type blade (202).
19. outer circulation type alkylation reactors as claimed in claim 4, it is characterised in that the quantity of described baffle plate (4) is 2～12；Or
The width of described baffle plate (4) is the 1/20～1/8 of the diameter of described big housing (304)；Or
The length of described baffle plate (4) is identical with the length of straight flange of big housing (304)；Or
The inwall of described baffle plate (4) and big housing (304) from span from for the 1/12～1/8 of baffle plate (4) width.
20. outer circulation type alkylation reactors as claimed in claim 19, it is characterised in that the quantity of described baffle plate (4) is 2-10 sheet.
21. outer circulation type alkylation reactors as claimed in claim 19, it is characterised in that multi-piece baffle plate (4) is equally distributed.
22. outer circulation type alkylation reactors as claimed in claim 19, it is characterised in that the width of described baffle plate (4) is the 1/12～1/10 of the diameter of described big housing (304).
23. outer circulation type alkylation reactors as claimed in claim 1, it is characterised in that described component distributor (6) includes charging aperture (601) and distributor pipe (602)；The upper distribution of described distributor pipe (602) is porose；Or
Described component distributor (6) is installed between described radial-flow type blade (202) and big end socket (305).
24. outer circulation type alkylation reactors as claimed in claim 23, it is characterised in that described component distributor (6) is tubular type distributor.
25. outer circulation type alkylation reactors as claimed in claim 23, it is characterised in that the ring diameter of described distributor pipe (602) is 0.8～1.2 times of described radial-flow type blade (202) diameter.
26. outer circulation type alkylation reactors as claimed in claim 23, it is characterized in that, the vertical dimension between described component distributor (6) and described radial-flow type blade (202) is 0.5～1.5 times of described radial-flow type blade (202) height.
27. outer circulation type alkylation reactors as claimed in claim 26, it is characterized in that, the vertical dimension between described component distributor (6) and described radial-flow type blade (202) is 0.8～1.2 times of described radial-flow type blade (202) height.
28. outer circulation type alkylation reactors as claimed in claim 1, it is characterised in that the top and bottom of described heat exchanger shell (13) are closed by end socket (15)；Or
Also include in described heat exchanger: tubulation gripper shoe (19), be used for fixing heat exchanging pipe (18).
29. outer circulation type alkylation reactors as claimed in claim 28, it is characterised in that described heat transferring medium import (16) and heat transferring medium outlet (17) are present on end socket (15).
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| CN105664826A (en) * | 2016-03-24 | 2016-06-15 | 华东理工大学 | External circulation type alkylation reactor and external circulation type alkylation reacting method |
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| CN105664826A (en) * | 2016-03-24 | 2016-06-15 | 华东理工大学 | External circulation type alkylation reactor and external circulation type alkylation reacting method |
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