KR20170081353A - Continuous stirred-tank reactor with panel - Google Patents

Abstract

The present invention provides a continuous stirred tank type reactor equipped with a panel.
Specifically, the continuous stirred tank type reactor of the present invention comprises: a reaction tank having an inlet and an outlet for introducing and discharging a raw material to one side, respectively; An agitator provided in the reaction vessel; And a continuous stirred tank reactor (CSTR) having a panel vertically installed on a wall surface of the reaction vessel, the panel being installed to be spaced apart from the stirring device by a predetermined distance.
Through the above structure, the continuous stirred tank type reactor of the present invention increases the residence time of the raw material introduced into the reaction tank during agitation, and significantly reduces the initial flow out amount and initial outflow concentration of the raw material.

Description

[0001] The present invention relates to a continuous stirred tank reactor

The present invention relates to a continuous stirred tank reactor capable of increasing the residence time of a raw material charged into a reaction tank and reducing initial discharge amount and concentration by having a panel.

Various types of reactors are used to uniformly stir raw materials in a large number of industrial synthesis and processing processes. In the process, the reactor is influenced by the concentration, temperature, pressure, time and catalyst of the reactant, so it is important to select the type of reactor most suitable for such process conditions.

As a generally used stirring reactor, there is typically a continuous anomaly reactor. The continuous anomaly reactor can again be divided into two models: a tubular reactor (PFR) and a continuous stirred tank reactor (CSTR).

Tubular reactors are those reactors that have the same flow as the flow of material in the reactor, as well as the shape of the reactor in the form of tubes. That is, the material introduced into the tubular reactor only mixes in the radial direction without axial mixing. At this time, the conditions in the reactor, such as temperature, composition, and flow rate, are constant based on one cross section of the reactor and vary continuously depending on the distance from the inlet.

Continuous Stirred Tank Reactor (CSTR), also called mixed flow reactor (MFR), is completely mixed when the feedstock is introduced into the reactor, resulting in a spatially homogeneous state and the temperature and concentration , The reaction rates are the same, the state of the reactor discharge stream is the same as that in the reactor, and there is no accumulation of material in the reactor as a continuous reactor operating in a steady-state.

Such a continuously stirred tank type reactor is used by continuously operating a stirring tank. The most representative example of the continuous stirred tank type reactor is a system in which the reaction raw materials are continuously supplied and discharged after being sufficiently evenly mixed in a single stirring tank. A liquid circulation pump may be installed to circulate and mix a sufficient amount of liquid through the tank.

Both of the tanks are mixed and stirred sufficiently evenly so that the liquid concentration is the same. Since the reaction proceeds continuously at a constant rate in this state, the reaction can be controlled and the reaction temperature can be easily maintained. .

In addition, instead of using one reaction tank, a method in which a plurality of reaction tanks are arranged in series to sequentially send reaction liquids (a series multistage tank-type reactor) requires a reactor volume necessary for performing a reaction It can be selected in a particularly advantageous manner when the throughput is large.

Indeed, the continuous stirred tank type reactor is used in various industrial fields, for example, for the purpose of producing a metallocene catalyst widely used in the process of producing synthetic materials such as polyethylene (PE) or polypropylene (PP) have.

Such a continuous stirred tank type reactor has advantages such as easy temperature control and the like, but also has a disadvantage of low conversion rate.

1 is a cross-sectional view of a conventional continuously stirred tank type reactor. 1, the continuous stirred tank reactor 200 includes a reaction tank 210 having an inlet and an outlet 220 for injecting / discharging a raw material, an agitator 211 in the reaction tank 210, .

Part of the reaction starting material injected into the reactor 200 having such a structure is stirred with a vortex and mixed into the tank (black dotted line in Fig. 1, green arrow in Fig. 2) As shown in FIG. 2, flows through the wall and flows out to the outlet (blue dotted line in FIG. 1) to continuously change the material composition and the material composition in the reaction tank. As a result, the final composition of the stirring product is unstable Problems to be solved occur.

To solve this problem and increase the conversion rate, the size of the reactor must be increased. Considering the economic and spatial limitations in installing the apparatus, there is a limit to increase the size of the reactor. In addition, the development and use of a completely new reactor structure is also inefficient because it would result in a complete reuse of the existing industrial facility.

Therefore, it was necessary to develop new technology that can easily manufacture and install, utilize the maximum amount of conventional industrial facilities, prevent the initial spillage of raw materials to be introduced, and significantly improve the efficiency of stirring efficiency.

A stirring-tank reactor system (Korean Patent Laid-Open No. 10-2007-0006864)

In order to solve the above-mentioned conventional problems, the inventors of the present invention have conducted various studies, and by installing a panel on the outlet side inside the reactor, it is possible to induce re-descent and remixing of the initial outflow, And the initial outflow amount of the raw material and the initial outflow concentration can be decreased. Thus, the present invention has been completed.

Accordingly, an object of the present invention is to increase the residence time of a raw material to be fed into a continuous stirred tank type reactor and to reduce an initial runoff amount and an initial runoff concentration of the raw material. Another object of the present invention is to achieve the above-described object without changing the structure of the conventional reactor as much as possible in consideration of practicality and economical efficiency.

In order to achieve the above object,

A reaction tank provided with an inlet and an outlet for supplying and discharging the raw material to one side, respectively;

An agitator provided in the reaction vessel; And

A continuous stirred tank reactor (CSTR) provided with a panel vertically installed on a wall surface of the reaction tank, the panel being installed to be spaced apart from the stirring device by a predetermined distance.

The continuous stirred tank type reactor of the present invention, from the structure shown in the above-mentioned task solution,

The initial runoff of the feedstock is re-lowered and remixed to increase the residence time of the feedstock in the reactor and reduce the initial runoff and initial runoff concentration. Further, as the residence time of the raw material in the reaction vessel increases, the mixing concentration and composition of the input raw materials can be stabilized more quickly.

The continuous stirred tank type reactor of the present invention is economical and practical because it has a remarkably improved effect as described above, and can be manufactured easily and easily in a line which does not change the conventional reactor structure as much as possible.

1 is a cross-sectional view of a conventional continuous stirred tank reactor without a panel.
FIG. 2 is a schematic top view showing the raw material flow in the reactor of FIG. 1; FIG.
3 is a perspective view of a continuous stirred tank type reactor having a panel according to the present invention.
4 is a perspective view of a panel according to an embodiment of the present invention.
FIG. 5 is a graph showing the concentration of the outflow raw material liquid over time in the case of conducting the stirring process from the reactor according to Example 1 of the present invention and Comparative Example. FIG.
FIG. 6 is a graph showing the concentration of the raw material liquid flowing out from the reactor according to Example 1 of the present invention and the comparative example over time (rpm increase) when the stirring process is performed at a high speed.
FIG. 7 is a graph showing the concentration of the outflow raw material liquid over time when the stirring process is carried out from the reactor according to the first and second embodiments of the present invention. FIG.

Hereinafter, the configuration of the present invention will be described in more detail with reference to Figs. 3 and 4. Fig.

3 and 4, only the most representative embodiments are described in order to facilitate understanding of the present invention. Therefore, the scope of the present invention is not limited thereto unless the specific configuration is specifically defined in the present specification And should be understood to cover all ranges equivalent to those described herein.

3 is a structure of an embodiment of a continuous stirred tank type reactor according to the present invention.

Referring to FIG. 3, the continuous stirred tank type reactor 100 according to the present invention includes a reaction tank 110, a stirring device 111, and a panel 112.

In the continuous stirred tank type reactor 100 of the present invention, the reaction tank 110 corresponds to a space where the panel 112 of the present invention is installed as a site where the raw materials for mixing are stirred.

The size and shape of the reaction vessel 110 may vary, and as is commonly used, a cylindrical reaction vessel 110 may be used. The size and shape of the reaction vessel 110 may affect the setting of the temperature and the flow rate set in the reactor 100 and the selection of the liquid or concentration of the input raw material.

An inlet 120 and an outlet 130 for injecting and discharging the raw material into the reaction tank 110 are provided on the side surface of the reaction tank 110.

The outlet 130 is usually located on the upper side of the reaction tank 110 and the inlet 120 may be located on the upper or lower side of the reaction tank 110. The inlet 120 and the outlet 120, 130, the specific height difference can be set in consideration of the intended use of the reactor 100 and the like.

It should be noted that such a substrate is meant to clearly specify that the effect of the present invention is not limited by the arrangement of the inlet port 120 and the outlet port 130. In practice, the continuous stirred tank reactor 200, The inlet 220 and the outlet 230 are installed at a high position in order to reduce the investment cost of the pump for transporting the raw material in the stirring process and the product is flowed out in an over flow type after the raw material is supplied. The inlet 120 and the outlet 130 may be provided on the uppermost side of the reaction tank 110, respectively, in order not to greatly change the structure.

In addition, the length and shape of the inlet 120 and the outlet 130 of the present invention may be changed according to the conventional structure and may be changed as required.

The stirrer 111 provided in the reaction tank 110 is a rod-shaped device for uniformly stirring the raw materials injected into the reaction tank 110 by generating a constant flow flow in the lower portion of the reaction tank 110. The stirring device 111 is located in the middle of the reaction tank 110 and takes into consideration various stirring conditions such as the nature of the raw material to be supplied, the concentration, the degree of stirring, the size of the reaction tank 110, and the temperature set in the reaction tank 110 The rotation speed (rpm) at which the stirring device 111 rotates can be adjusted.

A panel 112 for displaying the effect of the present invention is provided around the stirring device 111 in the reaction tank 110.

More specifically, the panel 112 is installed in a direction perpendicular to the wall surface of the reaction tank 110, and spaced apart from the agitation device 111 by a predetermined distance.

The panel is preferably installed between the outlet 130 and the agitator 111 so as to be parallel to the inlet 120 and the outlet 130. At this time, the proximity of the panel 112 to the outlet 130 can be set differently depending on the overall size of the panel 112 and / or the process conditions.

The panel 112 of the present invention is arranged in the reaction tank 110 to allow the flow of the raw materials that can be initially discharged to be re-lowered and remixed as indicated by a red dotted line in FIG. 3, Increasing the time and affecting the overall efficiency of the agitation.

In the present invention, the shape, size, thickness and width of the panel 112 are not limited to the specific form so long as the object of the present invention is not impaired. For example, Can be selected.

4 is a three-dimensional view showing a panel 112 according to an embodiment of the present invention. Referring to FIG. 4, the panel 112 may be a thin rectangular panel.

In particular, considering the structure and application examples of the conventional continuous stirred tank type reactor 100, the thickness of the panel 112 may preferably be 0.1 to 1 cm, 112 may be pushed by the flow of the raw material to interfere with the flow, so that the effect of the present invention can be reduced. When the amount exceeds the above range, it takes too much volume in the reaction tank 110, Because. However, the preferred thickness range is not necessarily limited, and as the process scale and the size of the reaction tank 110 are increased (scale-up), the thickness of the panel 112 can be made thicker.

The width of the panel 112 is preferably set to be less than the diameter of the outlet 110 of the outlet 130. If the width of the panel 120 is less than the above range, it is not possible to secure a sufficient area for re-lowering the flow of the raw material that is initially discharged. If the width exceeds the above range, the stirring device 111, This is because the placement is obstructed. In addition, even if the panel 112 can be disposed at the center of the reaction tank 110, if the panel 112 is excessively separated from the outlet 130, the influence on the initial outflow flow becomes insignificant.

Any material may be used as the material of the panel 112, as long as it does not react with the raw material introduced into the reaction tank 110, and does not affect the properties and stirring of the raw material. The width of the panel 112 may vary depending on the size and the ratio of the reaction tank 110 used.

When the panel 112 is arranged in the reaction tank 110, the height of the upper end may be set to 1/10 or more of the total length of the reaction tank 110 from the interface of the reaction tank 110, Can be more suitably prevented. The height of the lower end of the panel 112 is preferably as long as possible, and it is preferable to cover at least 1/4 of the lower portion of the reaction tank 110 including the interface. This is because when the panel 112 floats too high in the reaction tank 110, the influence of agitation at the lower part of the reaction tank 110 is insignificant and it is difficult to effectively prevent the flow of the raw material initially flowing out to the outlet 130 .

There is no limitation to the method of installing the panel 112 of the present invention in the reaction tank 110, and various fastening methods can be utilized. For example, a sliding groove may be provided on the inner wall of the reaction tank 110 so as to be fastened by a sliding method or a screw fastening method.

In summary, a Continuous Stirred Tank Reactor (CSTR, 100) is a continuous reactor for thoroughly mixing raw materials to be injected into a uniform state in space, , The reaction rate is the same and the state of the exhaust stream of the reactor 100 is the same as the state in the reaction tank 110. The continuous stirred tank type reactor 100 operates in a steady-state and does not leave any material accumulating in the reactor 100.

When the raw material is supplied to the inlet 120 of the reactor 100 to make a homogeneous mixture using the continuous stirred tank reactor 100, the raw material is stirred into the reactor 110.

At this time, the flow of the raw material flowing into the conventional continuously stirred tank type reactor 200 is indicated by the blue arrow and the black arrow in FIG. As shown in FIG. 1, some of the raw materials flowing into the vessel are wall-flowed and flow out toward the outlet 230 as shown by a blue arrow. Accordingly, the high-concentration raw material is hardly stirred at the initial stage When the continuous stirring tank type reactor 100 equipped with the panel 1120 of the present invention is used, the flow of the flow is disturbed by the panel 112, A kind of recycling occurs as indicated by the color dotted line. Accordingly, the flow of the raw material once again from the outlet 130 to the agitation region is generated, thereby increasing the retention time (RTD) of the raw material in the reaction tank 110. As a result, it is possible to reduce the initial outflow amount of the raw material and make the initial outflow concentration more uniform.

In addition, the reactor 100 of the present invention is remarkably improved in performance and is very economical and practical because it maximally utilizes the existing reactor structure and is easy to manufacture.

Hereinafter, Examples 1 to 2 and Comparative Examples and Experimental Examples 1 to 4 using them are described in order to facilitate understanding of the present invention. However, the following examples and experiments are only examples of the constitution and effect of the present invention, and the scope and effect of the present invention are not limited thereto.

< Example >

Example  One

One embodiment of the continuous stirred tank reactor structure 100 according to the present invention is as shown in FIG. A panel 112 is provided on the front surface of the outlet 130 in the cylindrical reaction tank 110. The length of the panel 112 includes the interface and does not contact the bottom surface of the reaction tank 110, 4 of the length of the reaction vessel 110 in the direction of the arrow. The inlet 120 and the outlet 130 are located on both sides of the upper part of the reaction vessel 110 and a stirrer 111 for stirring the raw materials flowing into the reaction vessel 110 is provided in the center of the reaction vessel 110.

Example  2

The continuous stirred tank type reactor 100 according to the second embodiment has the same structure as that of the reactor of the first embodiment. The length of the panel 112 includes an interface, and the bottom surface of the reaction tank 110 And was set so as to cover 3/4 of the length of the reaction tank 110 in the longitudinal direction while not contacting.

< Comparative Example >

This comparative example is a conventional continuous stirred tank type reactor 200 for the above Examples 1 and 2, as shown in Fig. The structure of the reactor 200 of this comparative example is the same as that of the reactor 100 shown in the first embodiment but differs from that of the reactor 100 in that a panel is not provided in the reactor 210.

< Experimental Example >

Experimental Example  1 - Difference in effect according to presence or absence of panel

In Experimental Example 1, experiments were conducted to confirm the initial runoff velocity and the concentration of the outflow materials when the raw materials were stirred using the continuous stirred tank type reactors of Example 1 and Comparative Example, respectively.

First, in order to carry out the experiment, the continuous stirring tank type reactor was stabilized, and the raw materials of certain components were put into the reactor through the inlet for 1 minute and stirred.

Subsequently, samples of the substances flowing into the outflow port were divided by time zone and UV analysis was performed. However, the use of the UV detector is intended only to easily check the tendency of the raw materials in the reactor, and the raw materials are not necessarily limited to specific components.

The results of each experiment obtained through the above UV analysis were quantified and converted into a graph of concentration distribution change over time as shown in FIG. 5 (a) corresponds to the results of the first and (b) comparative examples.

5 (a) and 5 (b), when the reactor of Example 1 is used, the slope of the overall graph is gentler than that of the comparative example.

Specifically, the initial concentration increase rate is slow, and the time taken to show the peak concentration of the outgoing raw material is also about 4 minutes, which is about 2 minutes slower than the comparative example. This is because the raw material to be discharged is recycled before being discharged by the panel structure. From the above results, it can be seen that when the reactor according to the embodiment is used, the time during which the raw materials to be supplied stay in the reactor is increased and the stirring efficiency is increased have.

In addition, the concentration peak of Example 1 exhibited a significantly lower value than that of the Comparative Example, and the gradient of the concentration decreasing from the concentration maximum was also gentler than that of the Comparative Example. From this, in Example 1, It can be confirmed that rapid concentration stabilization can be attained as it stays in the reactor for a long time.

For a more accurate comparative analysis, the standard deviation up to the maximum concentration point and the residence time in the reactor for the graphs of Example 1 and Comparative Example are mathematically calculated as shown in Table 1 below.

Standard deviation to maximum value Residence time Example 1 0.117 7.5 min Comparative Example 0.1679 5.1 min

As shown in the graph of FIG. 5, the residence time in the reactor is higher when the reactor of Example 1 is used, and the standard deviation before and after the maximum value is smaller in Example 1 .

According to the results of the present experimental example, it is possible to effectively prevent the outflow of the initial raw material from the reactor only by the provision of the panel in the reaction tank, thereby making it easy to control the concentration of the raw material in the reaction tank and to significantly improve the overall stirring efficiency .

Experimental Example  2 - Difference of effect according to panel length difference

In the above-described Experimental Example 1, it was confirmed that the stirring efficiency and performance were improved when the panel was provided in the reactor.

On the other hand, in Experiment 2, an experiment was conducted to confirm differences in the effect of panels having different lengths of panels.

For the experiment, the reactors of Examples 1 and 2 were used, in which the lengths of the panels were different from each other. The experimental method is the same as that of Experimental Example 1 described above, and each experiment result obtained through UV analysis is converted into a graph of concentration distribution change over time as shown in FIG. 6 (a) is a result of using the reactor of Example 1, and (b) is a result of using the reactor of Example 2. Fig.

 Referring to FIG. 6, in the case of using the reactor (b) of Embodiment 2 in which the length of the panels installed is relatively longer than that of (a) in the case of using the reactor of Embodiment 1, It can be confirmed that the graph has a slope graph. That is, when the length of the installed panel is long, it is confirmed that the efficiency of stirring in the reaction vessel is remarkably improved because the initial discharge rate is slow, the maximum concentration value of the discharged raw material liquid is small and the concentration gradient, which decreases from the maximum concentration point, have.

Since the continuously stirred tank type reactor of the present invention has remarkably improved stirring efficiency, it can be usefully used in various industrial fields requiring stirring products such as the production of metallocene catalysts.

100: continuous stirred tank type reactor of the present invention
110: Reactor
111: stirring device
112: Panel
120: inlet
130: Outlet
200: Conventional continuous stirring tank type reactor
210: Reactor
211: stirring device
220: inlet
230: Outlet

Claims (7)

A reaction tank provided with an inlet and an outlet for supplying and discharging the raw material to one side, respectively;
An agitator provided in the reaction vessel; And
A continuous stirred tank reactor (CSTR) provided in a vertical direction on a wall surface of the reaction tank, and having a panel installed at a predetermined distance from the stirring device.
The method according to claim 1,
Wherein the inlet and the outlet are located at an upper portion of the reaction tank.
The method according to claim 1,
Wherein the installation position of the panel is arranged to be horizontal with the inlet and the outlet.
The method according to claim 1,
Wherein the panel is installed at a height of 1/10 to 9/10 of the length of the reactor from the raw material interface in the reactor, and the total length is 1/4 to 3/4 of the length of the reactor.
The method according to claim 1,
Wherein the panel is disposed between an outlet and an agitating device.
The method according to claim 1,
Wherein the width of the panel is less than the diameter of the reaction vessel outside the width of the outlet.
The method according to claim 1,
Wherein the thickness of the panel is 0.1 to 1 cm.

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