CN105664745A - Delivery reinforced mechanical stirring type continuous emulsifier and emulsifying method - Google Patents

Abstract

The invention relates to a delivery reinforced mechanical stirring type continuous emulsifier and an emulsifying method. The delivery reinforced mechanical stirring type continuous emulsifier comprises a shell, a stirring driving motor, a stirring shaft, first axial-flow type blades, second axial-flow type blades, radial-flow type blades, barriers, a component distributor, a feed pipe and a discharge outlet. The delivery reinforced mechanical stirring type continuous emulsifier and the emulsifying method have the advantages that the fluid transportation and circulation flow capacity of systems can be reinforced by the aid of effects of the radial-flow type blades and the barriers and the axial-flow type blades mounted in different regions, accordingly, low-density and low-viscosity materials can be dispersed and emulsified in high-density viscous materials, and perfect emulsification effects can be realized.

Description

A mechanical agitation type continuous emulsifier and emulsification method for enhanced conveying

technical field

The invention belongs to the field of chemical equipment, and more specifically, the invention relates to a mechanically agitated continuous emulsifier and an emulsification method for enhanced transportation.

Background technique

Emulsification refers to the process of dispersing the dispersed phase in the continuous phase as fine droplets. One phase that is dispersed in an emulsion is called the dispersed phase or internal phase; the other phase is called the dispersion medium or external phase. Obviously, the inner phase is a discontinuous phase and the outer phase is a continuous phase. Mechanical equipment for preparing emulsions is known as an emulsifier or emulsifier. To prepare different emulsified products (emulsions), it is necessary to use different dispersed phases and continuous phases, and the emulsification equipment and emulsification conditions also need to be adjusted to achieve the desired emulsification effect.

For example, a typical alkylation reaction is the alkylation reaction of butane and butene to generate isooctane under the catalysis of concentrated sulfuric acid. In this sulfuric acid alkylation reaction, butene is dissolved in concentrated sulfuric acid as the continuous phase of the reaction system, while butane insoluble in concentrated sulfuric acid is the dispersed phase, and the alkylation reaction of butane and butene occurs at the interface between the two phases. superior. In order to improve the reaction efficiency, it is necessary to enhance its mass transfer area, and effectively dispersing alkanes in the concentrated sulfuric acid continuous phase is one of the important ways to enhance its mass transfer. However, because the solubility of the product isooctane and its corresponding isomerization products in concentrated sulfuric acid is low, and a large amount of unreacted alkane is used to improve the conversion rate of olefins, the alkane and product All need to be separated from the catalyst concentrated sulfuric acid as soon as possible to improve production efficiency. This requires that the dispersion and emulsification of alkanes in concentrated sulfuric acid does not require homogenization, but is suitable and controllable.

Patent CN204107349U discloses a new type of silicone oil emulsification reactor, in which anchor paddles, coils and high-shear emulsifiers are installed, the viscosity of silicone oil is reduced by heating, more paddles are added in the high-speed emulsification machine and the speed is increased And other measures to improve product emulsification uniformity. Patent CN204685014U discloses a high-shear emulsification device, which enhances the emulsification quality through the high-speed shearing action of the internal multi-layer zigzag disc after the jacket of the device is heated. Patent 201410184576.8 discloses an emulsification stirring device, which promotes up and down flow mixing through the cooperation of multi-axis frame type and blade type stirring to improve the effect. Patent CN201603524U discloses an emulsification device, which adopts a stirring blade provided with a through hole to emulsify the material in circulation to improve the emulsification effect. Patent 204447838U discloses a silicone oil emulsification device, which uses electromagnetic excitation to drive the rotating blades on the disc to achieve gentle and uniform stirring. Patent 202446992U provides a silicone oil emulsification and stirring device, which realizes the emulsification process with a small mixing force by means of a stirring column between coaxially fixed discs. Patent 102961987A provides a continuous high-viscosity silicone oil emulsification process with pre-mixing and its equipment. Equipment including pre-mixing screw pumps, static mixers, and emulsification stirring tanks are used to obtain high-viscosity silicone oil emulsification products. The emulsification stirring tank Pitched paddles with different number of blades are used in . The patent CN204247083U provides an emulsification device. Two reverse push wheels are installed on the emulsification machine shaft in the emulsification tank, which can effectively improve the emulsification capacity and make the emulsification more thorough and delicate. The patent CN204582987U provides an emulsifying machine, which is equipped with a plurality of stacked stirring impellers on the stirring shaft to cooperate with the stator. At the same time, the medium can be ultrasonically emulsified on the basis of mechanical emulsification through the side ultrasonic generator and the bottom ultrasonic generator. , the diameter of the emulsified medium is smaller and the emulsification effect is better. In the above-mentioned patents, the target product is a long-term stable emulsion product, which does not require product phase separation and does not contain chemical reactions. It is not suitable as a reaction system with chemical reactions and catalysts, such as sulfuric acid-catalyzed alkylation reaction systems. Disperse and emulsify.

专利CN104667856A、CN104549086A、CN104549115A、CN104549108A、CN104549116A、CN104549111A、CN104549110A、CN104549109A、CN104549087A、CN104549114A等在反应器内设置喷射混合构件及在反应器内安装旋转床或内外旋转床，以实现催化剂与反应物的分散mix. In this type of reactor, there are too many components to realize the dispersion and emulsification of the reaction system, and the installation is complicated, which is not convenient for the efficient manufacture of equipment.

Patent CN200520078557.3 discloses a horizontal alkylation reactor, which uses a propeller to integrate dispersion, mixing and heat exchange in the same equipment and carry out synchronously, but the shear dispersion, mixing and Flow heat transfer capacity is not considered adequately.

Patent CN103242895A discloses a C4 alkylation production method and device. The liquid phase C4 alkane and concentrated sulfuric acid are fully emulsified by a stirring device outside the device, and the alkylation reaction is completed in a multi-stage tower reactor. This patented method ensures the degree of emulsification of the acid hydrocarbons entering the reactor, but the interface renewal of the emulsion during the reaction process in the tower depends on the packing, and there are few timely control measures for it.

Patent CN203764234U discloses an alkylation reactor, which includes a top material inlet and distribution mixing section, a middle reaction section and a lower product separation section. The material distribution and mixing section uses a multi-pipe distributor to achieve uniform material distribution and mixing without an agitator; the reaction section is equipped with fillers to enhance the mass transfer effect and promote the reaction. The reactor can be directly cooled by gasification and heat removal. Too many material inlet pipelines are arranged in the material mixing section of the reactor, and the layout is complicated and the flow resistance is large, which is unfavorable for manufacturing, production and maintenance.

Patent CN102921368B discloses a horizontal internal circulation stirring reactor, which realizes the dispersion and circulation flow of materials by the combination of strong shear circulation flow blades and gradually changing width baffles. The power of material dispersion emulsification and circulation flow in the reactor is provided by the same paddle, which is not conducive to the regulation of emulsification requirements, and is also not conducive to the optimization of mass and heat transfer.

Therefore, this field also needs to develop upgraded equipment for dispersing and emulsifying low-density and low-viscosity materials (such as hydrocarbon organic matter) in high-density viscous materials (such as concentrated sulfuric acid).

Contents of the invention

The object of the present invention is to provide a mechanical stirring type continuous emulsifier and emulsification method with enhanced conveying.

In the first aspect of the present invention, there is provided a mechanically agitated continuous emulsifier for enhanced conveying, the emulsifier comprising: a housing 3; an agitating drive motor 1; an agitating shaft 2 driven by the agitating drive motor 1; An axial flow paddle 201, which is located on the stirring shaft; the second axial flow paddle 203, which is located on the stirring shaft; radial flow paddle 202, which is located on the first axial flow paddle 201 and the second axial flow paddle on the stirring shaft Between the two axial flow paddles 203; the baffle 4; the component distributor 6; the feed pipe 8;

In a preferred example, the mechanically agitated continuous emulsifier with enhanced transportation further includes: a heat exchange jacket 5 located on the outer wall of the shell; preferably, the heat exchange jacket 5 includes a semi-tubular heat exchange Coil pipe; material discharge port 7.

In another preferred example, the feed pipe 8 further includes a circulation feed pipe 9 .

In another preferred example, the tubes of the semi-tubular heat exchange coil are filled with a flowing liquid phase or a liquid phase heat exchange medium capable of phase change and vaporization.

In another preferred example, the material discharge port 7 can also be used as a feed port.

In another preferred example, the emulsifier housing 3 includes: an upper head 301; a cylinder 302; a lower head 303; preferably, the upper head 301 and the lower head 303 are ellipsoids Type head structure.

In another preferred example, the cylinder 302 is a straight cylinder.

In another preferred example, the discharge port 10 is located on the side wall of the barrel 302 .

In another preferred example, the feed pipe 8 and the circulation feed pipe 9 are located on the lower head 303 .

In another preferred example, the material discharge port 7 is located on the lower head 303 .

In another preferred example, the component distributor 6 passes through the housing 3 and enters the housing.

In another preferred example, the heat exchange jacket 5 covers the side wall of the cylinder 302 .

In another preferred example, the stirring shaft 2 passes through the upper sealing head 301 and is positioned in the lower sealing head 303 .

In another preferred example, the first axial-flow blade 201 and the second axial-flow blade 203 are selected from: propellers, airfoil paddles; preferably propellers.

In another preferred example, the diameters of the first axial-flow paddle 201 and the second axial-flow paddle 203 are 0.80-0.88 times, preferably 0.84-0.86 times, the diameter of the cylinder 302; and/or The above-mentioned first axial-flow paddle 201 is installed on the stirring shaft 2 at a position where the vertical distance from the upper bottom of the upper head 301 is 0.8-1.5 times, preferably 0.9-1.4 times, the diameter of the cylinder 302; and/or The second axial-flow paddle 203 is installed on the stirring shaft 2 at a position where the vertical distance from the lower bottom of the lower head 303 is 0.2-1.5 times, preferably 0.3-1.0 times, the diameter of the cylinder 302 .

In another preferred example, the radial flow blades 202 are selected from: straight-blade disc turbine paddles, symmetrical concave-blade disc turbine paddles, asymmetric concave-blade disc turbine paddles, and oblique blade paddles; preferably Disc turbine propeller.

In another preferred example, the radial flow blades 202 are one or more; preferably 1 to 5, such as 2 to 3; preferably, the plurality of radial flow blades The layer spacing is 0.8 to 1.5 times, preferably 0.9 to 1.2 times, the diameter of the radial flow blade 202; and/or the diameter of the radial flow blade 202 is 0.45 to 0.55 times the diameter of the cylinder 302, preferably 0.47 to 0.54 times.

In another preferred example, the number of the baffles 4 is 2-12 pieces; preferably 2-10 pieces; more preferably 2-8 pieces; such as 4 pieces, 6 pieces; preferably, Multiple baffle plates 4 are evenly distributed.

In another preferred example, the width of the baffle 4 is 1/20 to 1/8 of the diameter of the cylinder 302; preferably 1/12 to 1/10; or the baffle The length of 4 is the same as the length of the straight side of the cylinder 302; or the distance between the baffle 4 and the inner wall of the cylinder 302 is 1/12-1/8 of the width of the baffle 4.

In another preferred example, the component distributor 6 includes a feed inlet 601 and a distribution pipe 602; holes are distributed on the distribution pipe 602; preferably, the component distributor 6 is a circular Tube-type distributor; preferably, the diameter of the distribution pipe 602 is 0.8-1.2 times, more preferably 0.9-1.1 times, the diameter of the radial-flow paddle 202 .

In another preferred example, the component distributor 6 is installed between the radial flow paddle 202 and the second axial flow paddle 203; preferably, the component distributor 6 and the The vertical distance between the radial-flow paddles 202 is 0.5-1.5 times the height of the radial-flow paddles 202 , preferably 0.8-1.2 times.

In another preferred example, the diameter of the holes distributed on the distribution pipe 602 is 2-20 mm.

In another aspect of the present invention, the use of the mechanically agitated continuous emulsifier for enhanced delivery is provided, and the described mechanically agitated continuous emulsifier for enhanced delivery is used for emulsification of immiscible liquids; preferably, for Dispersion and emulsification of low-density and low-viscosity materials in high-density and viscous materials.

In another aspect of the present invention, there is provided a method for emulsifying using the mechanically agitated continuous emulsifier for enhanced delivery, the method comprising: providing the mechanically agitated continuous emulsifier for enhanced delivery, by The feed pipe 8 or the circulating feed pipe 9 input the continuous phase material into the cylinder 302; the dispersed phase material was input into the cylinder 302 through the component distributor 6; Under the combined action of the baffle plate 4, the cyclic shear dispersion enters the continuous phase material sucked and conveyed by the second axial flow paddle 203 (preferably, the continuous phase material can be continuously input), and is then absorbed by the first axial flow type After the paddle 201 is further dispersed and emulsified, it flows out of the emulsifier through the outlet 10 to obtain an emulsified product.

In a preferred example, the input volume flow ratio of the continuous phase and the dispersed phase into the emulsifier is: continuous phase:dispersed phase=1:1˜10:1.

In another preferred embodiment, during the emulsification process, an alkylation reaction occurs.

In another preferred embodiment, the dispersed phase is: hydrocarbons; preferably alkanes; more preferably C3-C5 alkanes, such as butane.

In another preferred embodiment, the continuous phase is sulfuric acid; for example, concentrated sulfuric acid; more specifically, concentrated sulfuric acid containing olefins (preferably C3-C5 olefins, such as butene).

Other aspects of the invention will be apparent to those skilled in the art from the disclosure herein.

Description of drawings

Fig. 1, a kind of mechanical agitation type continuous emulsifier structure schematic diagram (front view direction) of a kind of enhanced conveying of the present invention. In the figure, the dotted arrow indicates the flow direction of the liquid.

Figure 2. Schematic diagram of the structure of the circular tube distributor (top view direction).

Fig. 3. Structural schematic diagram of an emulsifier with a plurality of radial flow paddles installed on the stirring shaft (sectional view in the front view direction).

Figure 4. Schematic diagram of several radial flow blade structures. From left to right: straight blade disc turbine propeller, symmetrical concave blade disc turbine propeller, oblique blade propeller.

Figure 5. Schematic diagram of several axial-flow paddle structures. The upper left is an arc-shaped propeller, the upper middle is a fan-shaped propeller, the upper right is a four-blade airfoil propeller, the lower left is a six-blade airfoil propeller, the lower middle is a six-blade airfoil propeller, and the lower right is a k5 airfoil propeller.

In the figure, each reference sign is respectively:

1: Stirring drive motor;

2: stirring shaft; 201: first axial-flow paddle; 202: radial-flow paddle; 203: second axial-flow paddle;

3: shell; 301: upper head; 302: cylinder; 303: lower head.

4: baffle;

5: heat exchange jacket;

6: component distributor; 601: feed inlet; 602: distribution pipe;

7: Material discharge port (or feed pipe);

8: Feed pipe;

9: Circulation feed pipe;

10: Outlet.

detailed description

After in-depth research, the inventor provides a mechanically agitated continuous emulsifier with enhanced transportation, through the role of radial flow stirring blades and baffles, and by installing axial flow blades in different areas to strengthen the transportation of system fluids And circulating flow capacity, it can realize the dispersion and emulsification of low-density and low-viscosity materials in high-density and viscous materials, and the emulsification effect is very ideal.

the term

As used herein, the "low-density and low-viscosity material" refers to a type of material with relatively low density and low viscosity; for example, its density is generally 0.15-1 g/cm ³ , and its viscosity is generally 0.2-100CP. The "low-density and low-viscosity material" is used as the dispersed phase.

As used herein, the "high-density viscous material" refers to a type of material with relatively high density and high viscosity; for example, its density is generally 1-5 g/cm ³ or its viscosity is generally 1-1000CP. The "high-density viscous material" is used as the "continuous phase".

It should be understood that "low-density low-viscosity material" and "high-density viscous material" are relative concepts. For example, if the viscosity of the continuous phase is between 1 and 100CP (such as 20CP), the viscosity of the dispersed phase is lower than 1CP ( Such as 0.5CP), then the continuous phase is "high-density viscous material" relative to the dispersed phase.

Continuous emulsifier with mechanical agitation for enhanced delivery

The invention provides a mechanical agitation type continuous emulsifier with enhanced conveying. The emulsifier comprises: a shell, an agitation drive motor, an agitation shaft, a first axial flow paddle, a second axial flow paddle, a radial flow Type paddles, baffles, component distributors, feed pipes and outlets.

The shell includes: an upper head, a cylinder, and a lower head. The upper sealing head is used to close the upper end of the cylinder body, and the lower sealing head is used to close the lower end of the cylinder body, thereby forming an integral shell. As a preferred mode of the present invention, the upper head and the lower head are ellipsoidal head structures. As a preferred mode of the present invention, the cylinder is a straight cylinder.

The stirring drive motor is used to provide power for the operation of the stirring shaft, and any motor with appropriate driving capacity can be applied to the present invention. The stirring shaft passes through the upper sealing head and is positioned in the cylinder body or the lower sealing head. Usually, the main structure of the housing is cylindrical, and the stirring shaft is positioned on the centerline of the housing.

The first axial-flow paddle and the second axial-flow paddle are installed on the stirring shaft and located inside the barrel. As a preferred mode of the present invention, the diameters of the first axial-flow paddle and the second axial-flow paddle are 0.80-0.88 times, preferably 0.84-0.86 times, the diameter of the barrel. As a preferred mode of the present invention, the first axial-flow paddle is installed on the stirring shaft at a position where the vertical distance from the upper bottom of the upper head is 0.8 to 1.5 times, preferably 0.9 to 1.4 times, the diameter of the cylinder . As a preferred mode of the present invention, the second axial-flow paddle is installed on the stirring shaft at a position where the vertical distance from the lower bottom of the lower head is 0.2 to 1.5 times, preferably 0.3 to 1.0 times, the diameter of the cylinder . The axial-flow blade may be, but not limited to: a propeller or an airfoil; preferably a propeller. Figure 5 presents some axial flow paddles.

The radial-flow paddles are installed on the stirring shaft, and are located inside the cylinder between the first axial-flow paddles and the second axial-flow paddles. The radial flow blades can be one or more; preferably 1 to 5, such as 2 to 3; preferably, the layer spacing of the plurality of radial flow blades is the radial flow 0.8 to 1.5 times, preferably 0.9 to 1.2 times the diameter of the paddle. As a preferred mode of the present invention, the diameter of the radial flow blade is 0.45-0.55 times, preferably 0.47-0.54 times, the diameter of the barrel. The radial flow blades may be, but not limited to: straight-bladed disk turbine blades, symmetrical concave-bladed disk turbine blades, asymmetric concave-bladed disk turbine blades or oblique blades; preferably disk turbine blades. Figure 4 presents some radial flow paddles.

In order to cooperate with the radial-flow paddles, a baffle is provided near the inner side wall of the barrel of the present invention, so as to cooperate with the radial-flow paddles to cyclically shear and disperse the dispersed phase and enter the continuous phase. The number of baffles is at least 2 pieces; generally 2-12 pieces; preferably 2-10 pieces; more preferably 2-8 pieces, such as 4 pieces, 6 pieces. Generally, a plurality of baffles are evenly arranged around the wall of the cylinder close to the inner wall. As a preferred mode of the present invention, the distance between the baffle and the inner wall of the cylinder is 1/12-1/8 of the width of the baffle. As a preferred mode of the present invention, the width of the baffle is 1/20-1/8 of the diameter of the cylinder; preferably 1/12-1/10. As a preferred mode of the present invention, the length of the baffle is the same as the length of the straight side of the cylinder.

The emulsifier of the present invention also includes a heat exchange jacket located on the outer wall of the cylinder, which can be used to adjust the temperature of the liquid in the shell. As a preferred mode of the present invention, the heat exchange jacket includes a semi-pipe heat exchange coil, and the tube is filled with a flowing liquid phase or a liquid phase heat exchange medium capable of phase change and vaporization.

The emulsifier of the present invention also includes a component distributor, which is arranged in the cylinder, and includes a feed inlet and a distribution pipe, and holes are distributed on the distribution pipe. As a preferred mode of the present invention, the diameter of the holes distributed on the distribution pipe may be 2-20 mm. As a preferred mode of the present invention, the component distributor is a circular tube distributor. Preferably, the ring diameter of the distribution pipe of the component distributor is 0.8-1.2 times the diameter of the radial-flow paddle; more preferably 0.9-1.1 times. As a preferred mode of the present invention, the component distributor is installed between the radial flow paddle and the second axial flow paddle; preferably, the component distributor and the radial flow paddle The vertical distance between the blades is 0.5-1.5 times, preferably 0.8-1.2 times, the height of the radial flow blades.

The emulsifier according to the present invention also includes at least one feed pipe (feed inlet) and at least one discharge pipe (feed outlet).

The feed pipe is located on the cylinder body or the lower head; preferably at the bottom of the lower head. As a preferred mode of the present invention, the feed pipe vertically passes through the wall of the lower head; preferably, a circulation feed pipe is also provided on the feed pipe. The circulation feed pipe refers to a pipeline through which the substance in the emulsifier can circulate to another functional processing device (such as a heat exchanger).

The discharge port (discharge pipe) is located on the side wall of the cylinder, which is used to output the emulsified product; as a preferred mode of the present invention, the discharge port is located on the cylinder higher than the first axial flow The position of the paddle.

The emulsifier according to the present invention also includes a material discharge port, which is located at the bottom of the housing, and is used to discharge the remaining material in the emulsifier after the emulsification is completed. The material discharge port can also be used as a feed port.

Application of mechanically agitated continuous emulsifier with enhanced conveying

The present invention also provides the use of the mechanically agitated continuous emulsifier for enhanced transportation, which is used for emulsification of immiscible liquids; preferably, it is used for dispersing and emulsifying low-density and low-viscosity materials in high-density viscous materials .

The low-density and low-viscosity material is, for example, hydrocarbon organic matter, including alkanes; such as C3-C5 alkanes, more specifically butane.

The high-density viscous material is, for example, sulfuric acid, including concentrated sulfuric acid; more specifically, concentrated sulfuric acid containing olefins (such as C3-C5 olefins, such as butene).

The present invention also provides a method for emulsifying using the mechanically agitated continuous emulsifier for enhanced transportation of the present invention, comprising: providing the mechanically agitated continuous emulsifier for enhanced transportation, feeding the emulsifier through a feed pipe or a feed port The continuous phase material is input into the cylinder; the dispersed phase material is input into the cylinder through the component distributor; the stirring drive motor is turned on, and the dispersed phase material is cyclically sheared and dispersed under the joint action of the radial flow blade and the baffle, and enters the second shaft. The flow-type paddles are sucked into the conveyed continuous phase material, and then further dispersed and emulsified by the first axial-flow-type paddles, and then flow out of the emulsifier through the discharge port to obtain emulsified products.

When the mechanically agitated continuous emulsifier with enhanced conveying of the present invention is in operation, the rotation speed of the agitating drive motor is generally in the range of 100-800rpm, which is suitable. Of course, depending on the type and volume of the material to be emulsified, the rotational speed of the stirring can be adjusted to a value outside the above range, which is easily accomplished by those skilled in the art.

The method of the invention is suitable for dispersing and emulsifying low-density and low-viscosity materials in high-density and viscous materials. The method of the present invention is particularly suitable for the alkylation reaction that requires the participation of high-viscosity materials.

As a possible embodiment, the emulsifier of the present invention is suitable for emulsifiers and emulsification methods that use concentrated sulfuric acid as the continuous phase to disperse hydrocarbon medium. Concentrated sulfuric acid is a strong acidic inorganic acid, which is often used as a catalyst for organic reactions, such as catalyzing the alkylation of C3-C5 alkanes and olefins to generate high-octane fuel oil, that is, alkylated oil. High-octane alkylated oil is an important component of high-standard vehicle fuel oil, which plays an important role and significance in energy saving and emission reduction.

A typical alkylation reaction is the alkylation reaction of butane and butene to generate isooctane under the catalysis of concentrated sulfuric acid. In this sulfuric acid alkylation reaction, butene is dissolved in concentrated sulfuric acid as the continuous phase of the reaction system, while butane insoluble in concentrated sulfuric acid is the dispersed phase, and the alkylation reaction of butane and butene occurs at the interface between the two phases. superior. In order to improve the reaction efficiency, it is necessary to enhance its mass transfer area, and effectively dispersing alkanes in the concentrated sulfuric acid continuous phase is one of the important ways to enhance its mass transfer. However, because the solubility of the product isooctane and its corresponding isomerization products in concentrated sulfuric acid is low, and a large amount of unreacted alkane is used to improve the conversion rate of olefins, the alkane and product All need to be separated from the catalyst concentrated sulfuric acid as soon as possible to improve production efficiency. This requires that the dispersion and emulsification of alkanes in concentrated sulfuric acid does not require homogenization, but is suitable and controllable; the device of the present invention adjusts the shear dispersion ability of the blades to the dispersed phase by adjusting the structural form, diameter and stirring speed of the blades , to obtain a suitable droplet diameter of the dispersed emulsification, the droplet diameter of the dispersed phase corresponds to the time required for stabilization before the phase separation of the dispersed emulsification system in the subsequent process. At the same time, the alkylation reaction of butane and butene catalyzed by concentrated sulfuric acid is a strong exothermic reaction, and the system needs to control low temperature conditions, and the viscosity of concentrated sulfuric acid at low temperature is relatively high, so this emulsification includes heat transfer requirements. Dispersion process in viscous medium; the mechanically agitated continuous emulsifier with enhanced transportation of the present invention can realize temperature control through heat exchange jacket.

The main advantages of the present invention are:

(1) The radial-flow paddle with strong power input capacity is used to cooperate with the installed baffle to realize high-efficiency shearing and dispersion of materials and achieve a suitable degree of emulsification;

(2) While dispersing and emulsifying, the efficient update of the reaction interface is realized, the mass transfer effect is enhanced, and the reaction efficiency is improved;

(3) A semi-tubular heat exchange jacket is arranged on the outer wall of the reactor, which improves the heat transfer efficiency of the reaction heat;

(4) Axial-flow paddles that drive the flow of the reaction system are installed in the feed and discharge sections of the emulsifier, which strengthens the circulation and delivery capacity of the material fluid in the emulsifier, and also strengthens the ability to meet the requirements of the alkylation reaction. The ability to control the internal and external ratio of the required material cycle;

(5) Reasonable design of the diameter and rotation speed of the stirring blade is beneficial to control the emulsification effect and enhance the fluid transport capacity, so that it can not only meet the requirements of the mass transfer area of the reaction, but also enable the product and excess alkanes to be separated efficiently and improve production efficiency .

Below in conjunction with specific embodiment, further illustrate the present invention. It should be understood that these examples are only used to illustrate the present invention and are not intended to limit the scope of the present invention. For the experimental methods without specific conditions indicated in the following examples, the conventional conditions or the conditions suggested by the manufacturer are usually followed.

Embodiment 1, the mechanical agitation type continuous emulsifier of strengthening conveying

As shown in FIG. 1 and FIG. 3 , the mechanically agitated continuous emulsifier with enhanced transportation includes: a shell 3 ; an upper head 301 , a cylinder 302 , and a lower head 303 . The upper head 301 and the lower head 303 are ellipsoidal head structures.

The cylinder body 302 is a straight cylinder, and a heat exchange jacket 5 is arranged on its outer wall. The heat exchange jacket 5 includes a semi-tubular heat exchange coil, and the tube is filled with a flowing liquid phase or a liquid phase heat exchange device capable of phase change and vaporization. medium.

The stirring shaft 2 passes through the upper sealing head 301 and the cylinder body 302 , and is positioned in the lower sealing head 303 , and the stirring shaft 2 is driven by the stirring driving motor 1 .

On the stirring shaft 2 , a first axial-flow paddle 201 , a radial-flow paddle 202 and a second axial-flow paddle 203 are arranged.

The first axial-flow paddle 201 is located in the cylinder 302 and on the upper part of the radial-flow paddle 202. It is installed on the stirring shaft 2 and adopts a propeller whose diameter is 0.85 times the diameter of the cylinder.

The second axial-flow paddle 203 is located in the cylinder 302 and at the bottom of the radial-flow paddle 202. It is installed on the stirring shaft 2 and adopts a propeller whose diameter is 0.85 times the diameter of the cylinder.

The radial flow paddle 202 is located in the middle of the cylinder 302 and adopts a disc turbine blade whose diameter is 0.48 times the diameter of the cylinder 302 .

The barrel 302 includes a component distributor 6 which enters into the barrel 302 through the housing wall. The component distributor 6 is a circular pipe distributor, as shown in Figure 2, comprising a feed inlet 601 and a distribution pipe 602; the distribution pipe 602 is distributed with holes; the diameter of the distribution pipe 602 is 0.95 times the diameter of the radial flow paddle 202 . The diameter of the holes distributed on the distribution pipe 602 is 5mm. The component distributor 6 is installed between the radial flow paddle 202 and the second axial flow paddle 203 . The vertical distance between the component distributor 6 and the radial flow paddle 202 is equal to the height of the radial flow paddle 202 .

Baffles 4 are arranged inside the cylinder 302, and the baffles 4 are evenly arranged on the inner wall of the cylinder 302, the distance from the wall is 1/10 of the width of the baffles 4, and the number of installations is 6 pieces. The length of the baffle 4 is the same as the length of the straight side of the cylinder 302 , and the width is 1/11 of the diameter of the cylinder 302 .

The housing 3 is also provided with a plurality of material inlets and outlets, including a feed pipe 8 , a material outlet 10 , and a material discharge port 7 . The feed pipe 8 is also provided with a circulation feed pipe 9 . The outlet 10 is located on the side wall of the cylinder 302 . The feed pipe 8 is located on the lower head 303 . The material discharge port 7 is located on the lower head 303 .

Embodiment 2, the mechanical agitation type continuous emulsification method of strengthening conveying

1. Emulsification step

Simulated medium: syrupy saline solution is the continuous phase, and isooctane is the dispersed phase. The density ratio of the continuous phase to the dispersed phase is 1.5:1, and the viscosity ratio of the continuous phase to the dispersed phase is 80:1.

To simulate medium, utilize the mechanical stirring type continuous emulsifier described in embodiment 1 to carry out mechanical stirring type continuous emulsification, the steps are as follows:

In the mechanically agitated continuous emulsifier described in Embodiment 1, the continuous phase material is continuously input into the housing 3 through the feed pipe 8, and after the continuous phase material is immersed in the radial flow paddle 202, the stirring drive motor 1 is turned on, The rotating speed is 500rpm; then the dispersed phase material is continuously input into the cylinder 302 through the component distributor 6 (the input volume flow ratio is: continuous phase:dispersed phase=5:1).

The dispersed phase material is cyclically sheared and dispersed under the joint action of the radial flow paddle 202 and the baffle 4, enters the continuous phase material sucked and conveyed by the second axial flow paddle 203, and is then absorbed by the first axial flow paddle 201 After further dispersing and emulsifying, it flows out of the emulsifier through the discharge port 10 (this example adopts a simulated medium to simulate emulsification, and does not generate heat; when carrying out a heat-changing reaction such as an alkylation reaction, the emulsion that flows out continuously from the discharge port 10 The temperature is adjusted through the heat exchanger, so that the temperature is controlled within a suitable range, and then circulated back to the emulsifier). The emulsion that meets the requirements is collected from the discharge port 10.

After the emulsification process is finished, the material discharge port 7 can be opened to discharge the remaining material out of the emulsifier.

2. Emulsification result

(1) Examination of emulsification degree

Emulsification is carried out using the above method, and the time taken for phase separation of the emulsion by 50% is investigated. It is determined that the time required for 50% phase separation of the emulsion is 40-70 minutes.

It can be seen that in the mechanically agitated continuous emulsifier for enhanced transportation of the present invention, the radial flow paddle with strong power input capability is used to cooperate with the installed baffle plate, and the coordination effect of the axial flow paddle realizes the High-efficiency shear dispersion and achieve a suitable degree of emulsification.

(2) Investigation of emulsification efficiency

Emulsification is carried out by the above method, and the obtained emulsion is examined for the droplet diameter of the dispersed phase. It is determined that the content of the droplet diameter d ₃₂ <80 μm in the dispersed phase is greater than 80%. The diameter of the dispersed phase droplet is small, which is beneficial to improve the reaction efficiency.

It can be seen that the mechanically agitated continuous emulsifier of the present invention realizes efficient renewal of the reaction interface and enhances the mass transfer effect while dispersing and emulsifying.

(3) Inspection of material circulation parameters

During the emulsification process, the material circulation parameters were determined. It has been determined that the circulation flow rate calculated by the diameter of the axial flow blade is greater than 0.79.

It can be seen that the mechanically agitated continuous emulsifier of the present invention is provided with an axial-flow paddle that drives the flow of the reaction system, which strengthens the circulation delivery capacity of the material fluid in the emulsifier, and can meet the internal and external ratio of the material circulation required for the alkylation reaction. Regulatory ability.

(4) Stirring power consumption per unit volume of the dispersed emulsification system

It has been determined that the power consumption per unit volume of the dispersion emulsification system is in the range of 3-10kw/m ³ . It can be seen that the mechanically agitated continuous emulsifier with enhanced transportation of the present invention has very high production efficiency.

It can be seen from the above that while the present invention strengthens the circulation flow capability, the shear dispersion capability of the axial flow blade is improved. In view of the fact that excessive dispersion and emulsification will affect the phase separation performance, the diameter of the radial flow blade is adjusted reasonably, so as to realize the reasonable distribution of power consumption on the two blades, satisfy the dispersion and emulsification and strengthen the transportation, and the overall power consumption is stable.

It should be noted that the embodiments of the present invention are only used to illustrate the technical solutions of the present invention rather than limit the present invention. After reading the above teaching content of the present invention, those skilled in the art can make various changes or modifications to the present invention, and these equivalent forms also fall within the scope defined by the appended claims of the present application.

Claims (10)

1. the mechanical agitation type Continuous Emulsifier strengthening conveying, it is characterised in that described emulsator includes:

Housing (3);

Stirring drive motor (1);

Shaft (2), it is driven by stirring drive motor (1);

First axial-flow type blade (201), it is positioned on shaft;

Second axial-flow type blade (203), it is positioned on shaft;

Radial-flow type blade (202), it is positioned on shaft between the first axial-flow type blade (201) and the second axial-flow type blade (203);

Baffle plate (4);

Component distributor (6);

Feed pipe (8); With

Discharging opening (10).

2. the mechanical agitation type Continuous Emulsifier of strengthening conveying 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; It is preferred that this heat exchange jacket (5) includes half tubular heat exchange coil;

Material discharging hole (7); And/or

Described feed pipe (8) also includes recycle feed pipe (9).

3. the mechanical agitation type Continuous Emulsifier of strengthening conveying as claimed in claim 1, it is characterised in that described emulsator housing (3) including: upper cover (301); Cylinder (302); Low head (303); It is preferred that described upper cover (301) and low head (303) are spheroid shape end enclosure structure.

4. the mechanical agitation type Continuous Emulsifier of the strengthening conveying as described in as arbitrary in claim 1-3, it is characterised in that described discharging opening (10) is positioned at the sidewall of cylinder (302); Or

Described feed pipe (8) and recycle feed pipe (9) are positioned on low head (303); Or

Described material discharging hole (7) is positioned on low head (303); Or

Described component distributor (6) enters in housing through housing (3); Or

Described heat exchange jacket (5) is covered in the sidewall of cylinder (302); Or

Described shaft (2), through upper cover (301), is positioned in low head (303).

5. the mechanical agitation type Continuous Emulsifier of strengthening conveying as claimed in claim 1, it is characterised in that the first described axial-flow type blade (201) and the second axial-flow type blade (203) are selected from: propeller, Aerofoil impeller; It is preferably propeller; Or

The first described axial-flow type blade (201) and 0.80～0.88 times that diameter is cylinder (302) diameter of the second axial-flow type blade (203); Or

The first described axial-flow type blade (201) is installed on the position of 0.8～1.5 times that upper bottom portion vertical dimension is described cylinder (302) diameter of the upper distance upper cover (301) of shaft (2); Or

The second described axial-flow type blade (203) is installed on the position of 0.2～1.5 times that lower bottom part vertical dimension is described cylinder (302) diameter of the upper distance low head (303) of shaft (2).

6. the mechanical agitation type Continuous Emulsifier of strengthening conveying as claimed in claim 1, it is characterized 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; It is preferably disk vane wheel oar; Or

Described radial-flow type blade (202) is one or more; It is preferably 1～5; It is preferred that 0.8～1.5 times that the interlamellar spacing of described multiple radial-flow type blades is described radial-flow type blade (202) diameter; Or

0.45～0.55 times that diameter is cylinder (302) diameter of described radial-flow type blade (202).

7. the mechanical agitation type Continuous Emulsifier of strengthening conveying as claimed in claim 1, it is characterised in that the quantity of described baffle plate (4) is 2～12; It is preferably 2-10 sheet; It is preferred that multi-piece baffle plate (4) is equally distributed; Or

The 1/20～1/8 of the diameter that width is described cylinder (302) of described baffle plate (4); It is preferably 1/12～1/10; Or

The length of described baffle plate (4) is identical with the length of straight flange of cylinder (302); Or

The inwall of described baffle plate (4) and cylinder (302) from span from for the 1/12～1/8 of baffle plate (4) width.

8. the mechanical agitation type Continuous Emulsifier of strengthening conveying 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; It is preferred that described component distributor (6) is tubular type distributor; It is preferred that 0.8～1.2 times that the diameter of described distributor pipe (602) is described radial-flow type blade (202) diameter; Or

Described component distributor (6) is installed between described radial-flow type blade (202) and the second axial-flow type blade (203); It is preferred that 0.5～1.5 times that the vertical dimension between described component distributor (6) and described radial-flow type blade (202) is described radial-flow type blade (202) height, it is preferred that it is 0.8～1.2 times.

9. the purposes of the mechanical agitation type Continuous Emulsifier of the arbitrary described strengthening conveying of claim 1-8, it is characterised in that the mechanical agitation type Continuous Emulsifier of described strengthening conveying is for carrying out the emulsifying of immiscible liquid; It is preferred that for the dispersion and emulsion carrying out the low viscous material of low-density in high density viscous material.

10. the method that the mechanical agitation type Continuous Emulsifier utilizing the arbitrary described strengthening conveying of claim 1-8 carries out emulsifying, it is characterized in that, described method includes: the mechanical agitation type Continuous Emulsifier of the arbitrary described strengthening conveying of offer claim 1-8, inputs continuous phase material by feed pipe (8) or recycle feed pipe (9) in cylinder (302); In cylinder (302), dispersion phase material is inputted by component distributor (6); Open stirring drive motor (1), the circulation shear dispersion under the radial-flow type blade (202) combined effect with baffle plate (4) of dispersion phase material, entrance are sucked in the continuous phase material carried, again by after the first axial-flow type blade (201) further dispersion and emulsion by the second axial-flow type blade (203), emulsator is flowed out, it is thus achieved that emulsification product by discharging opening (10).