Continuous stirred tank reactor for aldol condensation reaction

Abstract

The continuous stirred tank reactor for aldol condensation reaction and the aldol condensation reaction device including the same according to the present invention have the effect of preventing the conversion rate from being reduced due to the generation of dead zones even when the equipment scale is expanded and bringing about high productivity, and have the effect of significantly increasing the reaction area during the reaction, inhibiting the layer separation of the aqueous phase and the organic layer, and significantly reducing the average particle size and the deviation of the organic layer particles dispersed in the aqueous phase. In addition, the catalyst content per unit yield is significantly reduced compared with the prior art, and the cost required for treating wastewater is significantly reduced compared with the prior art.

Description

Technical Field

[0001] The present invention relates to a continuous stirred tank reactor for aldol condensation reaction. Background Art

[0002] Generally, aldol condensation reaction refers to a process in which various olefins react with synthesis gas (CO / H2) in the presence of a metal catalyst and a ligand through a hydroformylation reaction called carbonyl synthesis (OXO) reaction to generate a linear or branched aldehyde with one or more carbon atoms added to the olefin, and then an aldol condensation reaction is performed to generate an α, β unsaturated aldehyde.

[0003] Unsaturated aldehydes synthesized by condensation reactions of aldols and the like can be converted into various acids or alcohols containing long-chain alkyl groups by oxidation or reduction reactions. Such alcohols or acids are used as solvents, additives, and raw materials for various plasticizers.

[0004] In the related art of the method for producing neopentyl glycol of Korean Publication No. 10-1996-0047519, a scheme of improving the reaction efficiency by providing an unreacted aldehyde recovery column after the aldol condensation reactor and circulating the unreacted product is disclosed. In addition, in the related art of the method for producing neopentyl glycol of Korean Publication No. 10-2004-0111873, a scheme of carrying out the aldol condensation reaction in two or more continuous stirred tank reactors (CSTR) arranged in series is disclosed.

[0005] However, in the past, when a continuous stirred tank reactor was used to synthesize an aldehyde compound into an unsaturated aldehyde by an aldol condensation reaction, in particular, when the reactor was expanded to achieve mass production, a dead zone, which indicates a region with poor mixing performance, was locally generated in a region inside the reactor. If a dead zone is generated inside the reactor, not only the conversion rate and yield are reduced, but also the reaction efficiency and energy efficiency are reduced, resulting in an increase in the scale of the equipment compared to the required conversion rate and yield, and there is a disadvantage of increased uncertainty due to the increase in variables caused by differences in theoretical design and the resulting increase in the frequency of problems.

[0006] Therefore, there is a demand for the development of a continuous stirred tank reactor for aldol condensation reaction which can minimize the dead zone generated inside the reactor, has a high conversion rate and yield, and is excellent in reaction efficiency and energy efficiency. Summary of the invention

[0007] An object of the present invention is to provide a continuous stirred tank reactor for aldol condensation reaction which can prevent a decrease in conversion rate due to the generation of a dead zone even when the equipment scale is expanded, thereby achieving high productivity and an aldol condensation reaction apparatus including the same.

[0008] Another object of the present invention is to provide a continuous stirred tank reactor for aldol condensation reaction, which significantly increases the reaction area during the reaction, inhibits the layer separation of the aqueous phase and the organic layer, and significantly reduces the average particle size and deviation of the organic layer particles dispersed in the aqueous phase, and an aldol condensation reaction device including the same.

[0009] Another object of the present invention is to provide a continuous stirred tank reactor for aldol condensation reaction and an aldol condensation reaction device including the same, which has a significantly lower catalyst content per unit yield than the prior art and significantly lower costs for treating wastewater than the prior art.

[0010] The continuous stirred tank reactor for aldol condensation reaction involved in the present invention is a bottom-up structure in which reactants flow from the bottom to the top, and is characterized in that it includes: a reactant flow inlet 100, which is arranged at the bottom of the reactor; a stirring section, which is arranged on the upper side of the above-mentioned reactant flow inlet 100 and includes multi-stage paddles separated from each other in the upper and lower directions; and an exhaust port 300, which is arranged on the upper side of the above-mentioned stirring section, and the above-mentioned multi-stage paddles are a pitched blade paddle located at the uppermost end, and a plurality of multi-stage flat blade paddles located at the lower end thereof.

[0011] In an example of the present invention, the stirring part may include a rotating shaft 240 connected to the multi-stage paddle, and the pitched blade paddle may include a plurality of pitched blades 210 twisted at an angle of 20 to 70 degrees based on the length direction of the rotating shaft 240 .

[0012] In an example of the present invention, the stirring part may include a rotating shaft 240 connected to the multi-stage paddle, and the flat-blade paddle may include a plurality of flat blades 220 formed at an angle of -10 to 10 degrees based on the length direction of the rotating shaft 240 .

[0013] A continuous stirred tank reactor for aldol condensation reaction according to an example of the present invention may further include an impact baffle 400, which is arranged at the lower side of the lowest flat-blade impeller in the above-mentioned multi-stage flat-blade impeller, so that the reactants flowing in from the above-mentioned inlet 100 collide and disperse to the outside of the reactor.

[0014] In an example of the present invention, the paddle may include a bracket 230 connecting the inclined blade 210 to the rotating shaft 240, and a ratio of a width d of the inclined blade 210 to a width D of the inside of the reactor may be 0.2 to 0.4.

[0015] In an example of the present invention, the paddle may include a bracket 230 connecting the oblique blades 210 to the rotating shaft 240, and the ratio of the width d of the flat blades 220 to the width D of the inside of the reactor may be 0.4 to 0.5.

[0016] In one example of the present invention, the stirring unit can disperse the reactants in the aqueous phase with an average particle size of 50 to 500 μm.

[0017] The aldol condensation reaction device involved in the present invention comprises the above-mentioned continuous stirred tank reactor for aldol condensation reaction.

[0018] The aldol condensation reaction device involved in the present invention may include: the above-mentioned continuous stirred tank reactor 10 for aldol condensation reaction; a plug flow reactor 20, into which reactants, catalysts and products flow from the above-mentioned continuous stirred tank reactor for aldol condensation reaction; and an oil-water separator 30, into which products and catalysts flow from the above-mentioned plug flow reactor, and the catalyst is separated into the water layer and the products are separated into the organic layer.

[0019] The continuous stirred tank reactor for aldol condensation reaction and the aldol condensation reaction apparatus including the same according to the present invention have the effect of preventing the conversion rate from decreasing due to the generation of dead zones even when the equipment scale is expanded, thereby bringing about high productivity.

[0020] The continuous stirred tank reactor for aldol condensation reaction and the aldol condensation reaction device including the same according to the present invention have the effects of significantly increasing the reaction surface area during the reaction, inhibiting the layer separation of the aqueous phase and the organic layer, and significantly reducing the average particle size and deviation of the organic layer particles dispersed in the aqueous phase.

[0021] The continuous stirred tank reactor for aldol condensation reaction and the aldol condensation reaction device including the same have the effect of significantly reducing the catalyst content per unit yield compared with the prior art, and significantly reducing the cost required for treating wastewater compared with the prior art. BRIEF DESCRIPTION OF THE DRAWINGS

[0022] Figure 1 This is a diagram showing a continuous stirred tank reactor for aldol condensation reaction according to the present invention.

[0023] Figure 2 This is a diagram specifically showing a stirring section provided inside the continuous stirred tank reactor for aldol condensation reaction according to the present invention.

[0024] Figure 3 This is a process flow diagram schematically showing an aldol condensation reaction apparatus including a continuous stirred tank reactor for aldol condensation reaction according to the present invention. DETAILED DESCRIPTION

[0025] Hereinafter, the continuous stirred tank reactor for aldol condensation reaction according to the present invention will be described in detail with reference to the accompanying drawings.

[0026] The drawings recorded in this specification are provided as examples in order to fully convey the concept of the present invention to those skilled in the art. Therefore, the present invention is not limited to the drawings provided, but can be embodied in other forms, and the drawings may be exaggerated in order to clarify the concept of the present invention.

[0027] The technical and scientific terms used in this specification have the meanings that are generally understood by those skilled in the art unless otherwise defined, and descriptions of well-known functions and structures that may unnecessarily confuse the main purpose of the present invention are omitted in the following description and drawings.

[0028] The singular form of the terms used in this specification can be construed as including the plural form unless otherwise indicated.

[0029] In the present specification, unless otherwise defined, the unit of % used without particular mention means weight %.

[0030] In the process of synthesizing an aldehyde-based reactant into an unsaturated aldehyde by an aldol condensation reaction, the reactants react in an aqueous phase containing a catalyst by a catalyst to synthesize a product, which is present on an organic layer and reacts in a liquid phase. Specifically When the batch equipment is expanded, a dead zone and layer separation are generated locally in a region inside the reactor, which leads to a decrease in conversion rate and yield, and a decrease in reaction efficiency and energy efficiency. In addition, compared with the required conversion rate and yield, there is a disadvantage of increased uncertainty due to the increase in variables caused by differences in theoretical design and the resulting increase in the frequency of problems.

[0031] Therefore, in order to improve the conversion rate and yield, it is necessary to reduce the size of the organic layer particles dispersed in the aqueous phase to increase the reaction surface area and minimize the formation of dead zones. However, in the past, even if the rotation speed of the impeller was increased, it was difficult to reduce the size of the organic layer particles, and there were problems such as increased layer separation. In addition, there were also limitations in minimizing the dead zone.

[0032] Therefore, the present invention provides a continuous stirred tank reactor having an internal structure of a specific shape described later, so that even if a batch production system is provided that can produce a large amount of products per unit time, it is possible to prevent the formation of dead zones inside the reactor during the reaction, which can significantly improve the conversion rate and yield, and the reaction surface area is large and the amount of catalyst used can be minimized.

[0033] The continuous stirred tank reactor for aldol condensation reaction involved in the present invention is a bottom-up structure reactor in which reactants flow from the bottom to the top, and is characterized by comprising: a reactant flow inlet 100, which is arranged at the bottom of the reactor; a stirring part, which is arranged on the upper side of the reactant flow inlet 100 and includes multi-stage paddles separated from each other in the upper and lower directions; and an outlet 300, which is arranged on the upper side of the stirring part, and the multi-stage paddles are a top pitched paddle at the top and a plurality of multi-stage flat paddles located at the lower end.

[0034] In the reactor, a mixture containing reactants and a catalyst flows into a reactant flow inlet 100 located at the lower part of the reactor, and the mixture is stirred and reacted while rising from the lower part to the upper part through the stirring part, and the mixture containing reactants and products is discharged through a discharge port 300 located at the upper part of the reactor, i.e., the upper part of the stirring part. Therefore, the volume fraction of the organic layer containing the product can be maintained lower, the layer separation phenomenon can be minimized, and the formation of a dead zone can be minimized.

[0035] At this time, the stirring section has a plurality of flat-blade paddles separated from each other at the lower part of the stirring section, and a separated pitched-blade paddle is arranged at the upper end of the stirring section, i.e., on the upper side of the flat-blade paddle arranged at the uppermost end among the plurality of flat-blade paddles. Therefore, the effect of preventing the layer separation phenomenon and the formation of a dead zone is achieved. In the past, there was a problem of layer separation and a dead zone formed at the uppermost end and the bottom of the reactor, but in the present invention, by locating the pitched-blade paddle at the upper part of the stirring section and locating the plurality of flat-blade paddles at the lower part of the stirring section, i.e., on the lower side of the pitched-blade paddle, it is possible to prevent the dead zone or layer separation that may be generated at the uppermost end of the reactor. In the case where the upper part, i.e., the uppermost end of the stirring section does not have a pitched-blade paddle, for example, in the case where the uppermost end of the stirring section has a flat-blade paddle, especially in the case where the capacity of the reactor is large, even if the stirring speed is increased, the layer separation phenomenon will occur, and a dead zone will be formed. On the contrary, due to the too fast stirring speed, the layer separation phenomenon may be further aggravated.

[0036] The reactor involved in the present invention is not limited as long as it is used for aldol condensation reaction. As an example, the reactant to be reacted can be an aldehyde compound such as n-Butylaldehyde, and the product can be an unsaturated aldehyde compound such as 2-ethylhexenal. However, this is only a specific and preferred example, and a variety of reactants can be used as long as they are reactants that can undergo aldol condensation reaction.

[0037] In the present invention, the catalyst used in order to react the reactant is not limited as long as it is a catalyst that can guide the aldol condensation reaction of the above-mentioned reactant. As an example, an alkaline or acidic catalyst can be used, for example, a basic catalyst is more preferably used. As the above-mentioned basic catalyst, any one or more catalysts selected from the NaOH aqueous solution and the KOH aqueous solution can be exemplified. However, this is only a specific and preferred example of the description, and the present invention is not necessarily limited to this for explanation.

[0038] The continuous stirred tank reactor for aldol condensation reaction according to a preferred example may further include an impingement baffle 400, which is arranged at the lower side of the flat blade impeller at the lowest end among the multi-stage flat blade impellers, and the reactants flowing in from the inlet 100 collide with the impingement baffle 400 and disperse to the outside of the reactor. As described above, by arranging the inclined blade impeller at the upper part of the stirring part, the dead zone and layer separation that may be generated at the uppermost end of the reactor are prevented, and at the same time, when the impingement baffle 400 is also provided, the layer separation and dead zone that may be generated at the lowermost end of the stirring part can also be prevented. More specifically, when the impingement baffle 400 is further provided at the lower part of the reactor, i.e., at the lower side of the flat blade impeller at the lowest end among the plurality of flat blade impellers, the mixture containing the reactants and the catalyst flowing in from the reactant inlet 100 collides with the impingement baffle 400 and disperses to the outside of the reactor, i.e., the inner wall of the reactor, and while being dispersed, the mixture rises to the upper part of the reactor, and is stirred and reacted by passing through the flat blade impeller and the inclined blade impeller in sequence. Therefore, layer separation and a dead zone which may be generated at the lowermost end of the reactor are prevented.

[0039] The impact baffle 400 may be formed in a structure that is separated from and covers the reactant inlet 100 so that the mixture containing reactants and catalysts flowing from the reactant inlet 100 collides and is dispersed toward the inner wall surface of the reactor.

[0040] The distance between the impact baffle 400 and the flat-blade paddle, and the distance between the impact baffle 400 and the reactant stream inlet 100 can be appropriately adjusted according to the height of the reaction space of the reactor and the position of the reactant stream inlet 100. As a preferred example, the distance between the impact baffle 400 and the flat-blade paddle can be 4 to 26 cm, and the distance between the impact baffle 400 and the reactant stream inlet 100 can be 2 to 26 cm, but the present invention is not limited thereto.

[0041] There is no limitation on the fixing mechanism of the impact baffle 400 as long as it can be fixed at a position spaced from the lower side of the lowest flat-blade propeller among the flat-blade propellers. Figure 1As shown, the impact baffle 400 can be connected to the lowermost end of the rotating shaft 240. Although not shown in the drawings, the impact baffle 400 can also be connected and fixed to the inner wall surface of the reactor. However, this is only described as a preferred example, and the present invention is not necessarily limited to this for interpretation.

[0042] The stirring part may include a rotating shaft 240 connected to the multi-stage paddle. Figure 2 As shown, a plurality of paddles are connected to the rotating shaft 240 in a manner spaced apart from each other in the up-down direction, and agitation is performed by rotation.

[0043] like Figure 2 As shown, the above-mentioned pitched-blade paddle is in a state of being twisted at a prescribed angle based on the length direction of the rotating shaft 240. As for its specific shape and structure, since it is widely known in the technical fields related to impellers, blades, and agitators, it can be referred to. As a preferred example, the above-mentioned pitched-blade paddle can include a plurality of pitched blades 210 formed by twisting at an angle of 20 to 70 degrees, specifically 30 to 60 degrees, more specifically 35 to 55 degrees, and as an embodiment, 45 degrees based on the length direction of the rotating shaft 240. In this case, the number of blades can be more than 2, and specifically, 2 to 6 can be cited. In addition, the twisting directions of the angles of the plurality of blades can be the same direction as each other or different directions from each other, but preferably the same direction as each other.

[0044] like Figure 2 As shown, the flat blade paddle may include a plurality of flat blades 220 formed at -10 to 10 degrees based on the length direction of the rotating shaft 240. As for its specific shape and structure, since it is well known in the technical fields related to impellers, blades, and stirring parts, it can be referred to. As a preferred example, the flat blade paddle may include a plurality of blades formed at -10 to 10 degrees, specifically -5 to 5 degrees, and as an embodiment, 0 degrees (parallel to the length direction of the rotating shaft) based on the length direction of the rotating shaft 240. At this time, the number of blades may be more than 2, and specifically, 2 to 6 may be cited.

[0045] The paddle may have a structure including a bracket 230 for connecting the inclined blade 210 or the flat blade 220 to the rotating shaft 240. The bracket 230 has no great restrictions on its shape and structure as long as it is a mechanism for connecting and fixing the inclined blade 210 or the flat blade 220. For example, the bracket 230 may be a member having a diameter smaller than the length of the blade in the vertical direction corresponding to the rotating shaft 240, and more preferably, may be in the shape of a rod having a diameter whose stirring force (lift) is practically negligible compared to that of the blade.

[0046] As a preferred example, refer to Figure 1The ratio of the width d of the inclined blade 210 to the width D of the reactor interior is preferably 0.2 to 0.4, and the ratio of the width d of the flat blade 220 to the width D of the reactor interior is preferably 0.4 to 0.5. When this range is met, the probability of layer separation and dead zone generation can be further reduced, and the above effect can be further improved.

[0047] As a preferred example, the above-mentioned flat-blade paddles are preferably provided with three or more separated from each other on the lower side of the above-mentioned inclined-blade paddles, specifically, 3 to 9 separated from each other, and more specifically, 3 to 5 separated from each other, which is more preferred in terms of further improving the above-mentioned effects.

[0048] The reaction zone volume of the continuous stirred tank reactor according to one embodiment of the present invention can be appropriately adjusted according to the scale. As an example, 0.6 to 1 m 3 Of course, the present invention is not limited to this for explanation.

[0049] The distance between the paddles (based on the vertical direction of the rotating shaft) can be appropriately adjusted according to the scale of the reactor, specifically the volume of the reaction zone, and can be 10 to 50 cm based on the volume of the reaction zone. In addition, the distance between the flat-blade paddles (based on the vertical direction of the rotating shaft) can be appropriately adjusted according to the scale of the reactor, specifically the volume of the reaction zone, and can be 10 to 60 cm based on the volume of the reaction zone.

[0050] The reactants in the mixture containing the reactants and the catalyst flowing into the stirring part react in the form of being dispersed in a very small size in the aqueous phase, specifically, dispersed in an average particle size of 50 to 500 μm, more specifically 100 to 400 μm.

[0051] In addition, the present invention provides an aldol condensation reaction device including the above-mentioned continuous stirred tank reactor for aldol condensation reaction. Specifically, Figure 3 As shown, the aldol condensation reaction device may include: the above-mentioned continuous stirred tank reactor 10 for aldol condensation reaction; a piston flow reactor 20, into which reactants, catalysts and products flow from the above-mentioned continuous stirred tank reactor for aldol condensation reaction; and an oil-water separator 30, into which products and catalysts flow from the above-mentioned piston flow reactor, and the catalyst is separated into the water layer and the products are separated into the organic layer.

[0052] Even if the aldol condensation reaction apparatus involved in the present invention is expanded to meet the required production volume, the amount of additional space to be secured is not large compared with the prior art, and the average particle size of the organic layer particles dispersed in the water layer during the reaction can be minimized, and such a reaction state can be maintained in the entire area inside the reactor. Not only is the reaction area and efficiency high, but even with an expanded batch production system, the effect of low uncertainty and high-precision process control can be achieved.

[0053] The aldol condensation reaction apparatus involved in the present invention has the effect of synthesizing a product with a high conversion rate and yield by continuously circulating through the continuous stirred tank reactor 10, the plug flow reactor 20 and the oil-water separator 30, so that the catalyst separated into the water layer in the above-mentioned oil-water separator 30 directly flows into the above-mentioned continuous stirred tank reactor 10 for circulation.

[0054] Preferably, the aldol condensation reaction device further includes a heat exchanger that transfers the heat of the product to the reactants flowing into the continuous stirred tank reactor 10. Therefore, the catalyst separated into the water layer in the oil-water separator 30 directly flows into the continuous stirred tank reactor 10 and circulates, and the high heat of the product is not discarded as waste heat, but the heat is transferred to the reactants, thereby having the effect of synthesizing the product with a higher conversion rate and yield even in a batch production system larger in scale than the prior art.

[0055] Preferably, the catalyst separated into the water layer in the oil-water separator 30 flows directly into the continuous stirred tank reactor 10. “The catalyst separated into the water layer in the oil-water separator 30 flows directly into the continuous stirred tank reactor 10 and circulates” means that the catalyst circulating through the oil-water separator 30 does not flow into the reactor through the supply line for transferring the reactants, but flows into the continuous stirred tank reactor 10. That is, in the present invention, the circulating catalyst does not flow into the supply line for transferring the reactants, but flows into the continuous stirred tank reactor 10 in a state where the catalyst is mixed with the mixture. As in the prior art, when the catalyst circulating through the oil-water separator 30 flows into the continuous stirred tank reactor 10 through the mixing supply line after mixing with the reactants, especially in the case of a mass production system that is expanded and has a large volume of the reaction area, it is difficult to maintain the reaction state in which the average particle size of the organic layer particles dispersed in the water layer during the reaction is minimized in the entire area inside the reactor because it is actually difficult to accurately control the process conditions. As a result, the conversion rate and yield, that is, the production volume may be reduced. The aldol condensation reaction in which reactants are synthesized into products by means of a catalyst is preferably carried out inside a reactor having an environment that satisfies the process conditions. If the reaction is carried out in an environment that does not satisfy the above conditions, i.e., a mixed supply pipeline, etc., it is difficult to control the process due to the effects of multiple variables, and the uncertainty increases, making it difficult to achieve a conversion rate above the required level.

[0056] The plug flow reactor (PFR) 20 can be easily designed with reference to known literature. As an example, the interior of the reactor can have a spiral continuous component with a constant or non-constant pitch along the length of the tube. Of course, the present invention is not limited to this.

[0057] The reaction temperature of the continuous stirred tank reactor 10 or the plug flow reactor 20 can be set to 80 to 200° C., specifically, 100 to 160° C., with reference to known literature. That is, the aldol condensation reaction apparatus according to one example of the present invention may further include a temperature regulating unit that controls the reaction temperature of each reactor 10, 20 to 50 to 150° C.

[0058] The oil-water separator 30 is a device for separating an upper organic layer and a lower water layer from a mixture containing a catalyst and a product. The details thereof can be referred to known documents. Products such as 2-ethylhexenal exist in the organic layer, and a catalyst exists in the water layer. 2-ethylhexenal is discharged through an upper pipe of the oil-water separator 30, and 2-ethylhexenal is discharged through a lower pipe of the oil-water separator 30.

[0059] In the continuous stirred tank reactor 10, the conversion rate may be 30% to 60%, specifically preferably in the range of 35% to 55%, and in the plug flow reactor 20, the conversion rate may be 95% or more, specifically 97% or more, more specifically in the range of 97% to 99.9%. When the conversion rates in the continuous stirred tank reactor 10 and the plug flow reactor 20 meet the above ranges, respectively, a high conversion rate and yield of 95% or more, preferably 97% or more, can be achieved in the end.

[0060] That is, the aldol condensation reaction apparatus involved in a preferred example may also include a residence time control unit so that the conversion rate in the continuous stirred tank reactor 10 is 30% to 60%, specifically 35% to 55%, and the conversion rate in the plug flow reactor 20 is 95% or more, specifically 97% or more, and more specifically 97% to 99.9%.

[0061] The residence time control unit can adjust the residence time of the continuous stirred tank reactor 10 or the plug flow reactor 20. The residence time can be appropriately controlled to meet the conversion rate. For example, the residence time can be adjusted to 1 second to 10 minutes, specifically, 10 seconds to 5 minutes. However, this is only a preferred example, and the present invention is not necessarily limited to this for interpretation.

[0062] The reaction pressure of the continuous stirred tank reactor 10 or the plug flow reactor 20 can be determined by referring to known literatures, and as an example, can be 1 to 50 bar, specifically, can be in the range of 2 to 10 bar. That is, the aldol condensation reaction apparatus according to an example of the present invention can further include a pressure regulating unit for controlling the pressure of each reactor 10, 20 within the above range.

[0063] In the present invention, reactants react in a liquid phase through a catalyst to synthesize a product, and the reaction is carried out in a liquid phase, and a solution containing reactants, catalysts and / or products can be transferred by a pump. The position of the pump is not particularly limited, and as an example, it can be set between the continuous stirred tank reactor 10 and the plug flow reactor 20. However, this is only an explanation as a specific example, and the present invention is not necessarily limited to this for interpretation.

[0064] In the continuous stirred tank reactor 10 or the plug flow reactor 20, the flow rate of the solution containing the reactants, catalyst and / or product can be referred to in known literature. As an example, it can be 50 to 200 m / s. 3 That is, the aldol reaction apparatus according to one example of the present invention may further include a flow rate regulator for controlling the flow rate of the solution in each reactor 10, 20 within the above range.

Claims

1. A continuous stirred tank reactor for aldol condensation reaction, which has a bottom-up structure in which reactants flow from the bottom to the top, It is characterized in that include: A reactant stream inlet (100) is disposed at the lower portion of the reactor; a stirring portion, disposed on the upper side of the reactant stream inlet (100), comprising a plurality of paddles spaced apart from each other in the up-down direction; and The discharge port (300) is arranged on the upper side of the stirring part. The multi-stage propeller is a pitch-blade propeller at the top and three or more multi-stage flat-blade propellers at the bottom. The reactor further comprises an impact baffle (400), which is arranged at the lower side of the lowest flat-blade impeller in the multi-stage flat-blade impeller, so as to cause the reactants flowing in from the inlet (100) to collide and disperse toward the outside of the reactor. The stirring part includes a rotating shaft (240) connected to the multi-stage paddle. The pitched blade paddle comprises two or more pitched blades (210) twisted at an angle of 20 to 70 degrees based on the length direction of the rotating shaft (240), and The flat-blade paddle includes two or more flat blades (220) formed at an angle of -10 to 10 degrees with respect to the longitudinal direction of the rotation axis (240).

2. The continuously stirred tank reactor for aldol condensation reaction according to claim 1, wherein The paddle includes a bracket (230) connecting the oblique blade (210) to a rotating shaft (240), The ratio of the width (d) of the inclined blade (210) to the width (D) of the interior of the reactor is 0.2 to 0.

4.

3. The continuously stirred tank reactor for aldol condensation reaction according to claim 1, wherein The paddle includes a bracket (230) connecting a flat blade (220) to a rotating shaft (240), The ratio of the width (d) of the flat blade (220) to the width (D) of the interior of the reactor is 0.4 to 0.

5.

4. The continuously stirred tank reactor for aldol condensation reaction according to claim 1, wherein The stirring section disperses the reactants in the aqueous phase with an average particle size of 50 to 500 μm.

5. An aldol condensation reaction device, wherein: A continuously stirred tank reactor for aldol condensation reaction comprising the reactor described in any one of claims 1 to 4.

6. The aldol condensation reaction device according to claim 5, in, include: The aldol condensation reaction is carried out using a continuous stirred tank reactor (10); a plug flow reactor (20) for reactants, catalysts and products to flow from the continuous stirred tank reactor for aldol condensation reaction; and The oil-water separator (30) allows the product and the catalyst to flow from the plug flow reactor, separates the catalyst into the water layer, and separates the product into the organic layer.

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