Reactive monomer separation apparatus

Abstract

The present invention relates to a separation apparatus, and more particularly to a separation apparatus in which the structure of the feed supply unit is designed to enable uniform distribution of the feed within the column, thereby improving column efficiency.

Description

[[Technical Field]]

[0001] This application claims the benefit of priority based on Korean Patent Application No. 10-2023-0124667 filed on September 19, 2023, and all contents disclosed in the documents of the corresponding Korean patent application are incorporated as a part of the present specification.

[0002] The present invention relates to a separation device, and more particularly, to a separation device that improves column efficiency by designing the structure of a feed supply unit such that a feed in a column is uniformly distributed. Technical Field of the Invention

[0003] A dual flow tray is a distillation device designed such that, in a configuration having no downcomer, gas and liquid move upward and downward through holes to come into contact with each other. Specifically, a dual flow tray has no downcomer, a liquid flow is generated by liquid weeping from holes in the tray, and the dual flow tray is used when a substance to be separated undergoes severe polymerization inside a column to form a polymer, and fouling is a concern.

[0004] A dual flow tray has advantages of having a large allowable flow rate and being capable of coping with polymer fouling, but has a disadvantage of lower efficiency than columns using other conventional types of trays due to a channeling phenomenon that occurs when fluid flows without exchange between liquid and vapor. The channeling phenomenon is a main factor that reduces column efficiency, and the larger the diameter of the column, the more likely the channeling phenomenon tends to occur.

[0005] Channeling is a phenomenon in which uneven flow of liquid and gas occurs due to physical factors such as non-uniform feed distribution and tray clogging. When channeling occurs, the gas-liquid contact area is reduced, and consequently, gas-liquid contact occurs in a region smaller than the design capacity. Furthermore, dual-float trays lack a lowering plate, preventing liquid redistribution, which reduces the overall efficiency of the column, leading to problems such as decreased product quality and increased energy consumption.

[0006] Thus, in columns using dual float trays, the non-uniform distribution of feed within the column causes channeling phenomena. Therefore, uniform feed distribution is one of the factors determining column efficiency. However, conventionally, columns have been designed without considering uniform feed distribution within the column, resulting in low efficiency. Consequently, it is necessary to design a feed supply structure that enables uniform feed distribution in columns using dual float trays. [Overview of the Initiative] [Problems that the invention aims to solve]

[0007] The problem that this invention aims to solve is to provide a reactive monomer separation apparatus with improved column efficiency by designing the structure of the feed supply unit so that the feed can be uniformly distributed within the column, in order to solve the problems mentioned in the background art of the invention described above.

[0008] However, the problems that this application seeks to solve are not limited to those mentioned above, and other problems not mentioned can be clearly understood by an ordinary engineer from the following description. [Means for solving the problem]

[0009] A reactive monomer separation apparatus according to one embodiment of the present invention, which solves the above problems, includes a cylindrical column, a plurality of dual float trays provided inside the cylindrical column and dividing a plurality of stages, and a feed supply unit provided in one of the plurality of stages and supplying a raw material containing a liquid-phase reactive monomer.

[0010] Furthermore, the feed supply unit is spaced apart between the lower dual float tray and the upper dual float tray of the stage on which the feed supply unit is provided, and includes a circular feed transfer pipe provided along the inner wall of the cylindrical column, a plurality of inner pipes extending from the feed transfer pipe in the direction of the central axis, and a plurality of injection nozzles provided in the plurality of inner pipes, each of the plurality of inner pipes being individually equipped with a plurality of injection nozzles. [Effects of the Invention]

[0011] The reactive monomer separation apparatus according to the present invention prevents fouling by using a dual float tray, maximizes the feed distribution area of ​​the feed stage with the dual float tray, and designs the structure of the feed supply section to uniformly supply the raw material, thereby preventing channeling phenomena, maximizing the gas-liquid contact area, and increasing the overall efficiency of the column.

[0012] More specifically, the reactive monomer separation apparatus according to the present invention improves the separation efficiency of the column and enhances the quality of the final product obtained by improving the structure of the feed supply section so that the feed can be uniformly distributed in a dual float tray and preventing the channeling phenomenon, thereby also reducing energy consumption.

[0013] The effects obtained in this application are not limited to those mentioned above, and any further effects not mentioned can be clearly understood by a person with ordinary skill in the art to which this invention pertains from the following description. [Brief explanation of the drawing]

[0014] [Figure 1] This is a cross-sectional view of a separation apparatus for reactive monomers according to one embodiment of the present invention. [Figure 2] As a perspective view illustrating the detailed structure of area A in Figure 1 according to one embodiment of the present invention, a feed supply unit equipped with an injection nozzle at the lower part of a straight inner pipe is shown. [Figure 3] As a perspective view illustrating the detailed structure of area A in Figure 1 according to one embodiment of the present invention, a feed supply unit equipped with an injection nozzle at the lower part of a branched inner pipe is shown. [Figure 4] As a perspective view illustrating the detailed structure of area A in Figure 1 according to one embodiment of the present invention, a feed supply unit equipped with an injection nozzle at the top of a straight inner pipe is shown. [Figure 5] As a perspective view illustrating the detailed structure of area A in Figure 1 according to one embodiment of the present invention, a feed supply unit equipped with an injection nozzle at the top of a branched inner pipe is shown. [Figure 6] This is a perspective view illustrating a feed injection system equipped with six straight internal pipes, as one embodiment of the present invention. [Figure 7] This is a top view illustrating the feed injection region B formed in a dual float tray when six linear internal pipes are provided as one embodiment of the present invention. [Figure 8] This is a perspective view illustrating a feed injection system with two branched internal pipes, as one embodiment of the present invention. [Figure 9] This is a top view illustrating a feed injection area B formed in a dual float tray when two branched internal pipes are provided as one embodiment of the present invention. [Figure 10] This is a perspective view illustrating a feed injection system with three branched internal pipes, as one embodiment of the present invention. [Figure 11] This is a top view illustrating a feed injection region B formed in a dual float tray when three branched internal pipes are provided as one embodiment of the present invention. [Figure 12]As one embodiment of the present invention, this is a perspective view illustrating feed injection when four branched inner pipes are provided. [Figure 13] As one embodiment of the present invention, this is a top view illustrating feed injection region B formed on a dual flow tray when four branched inner pipes are provided. [Figure 14] As one comparative example of the present invention, this is a perspective view illustrating feed injection when each of four inner pipes is provided with only one injection nozzle. [Figure 15] As one comparative example of the present invention, this is a top view illustrating a feed injection region formed on a dual flow tray when each of four inner pipes is provided with only one injection nozzle. [Figure 16] As one embodiment of the present invention, this is a side view illustrating feed injection region B when injection nozzles are provided in a form inclined at a predetermined angle. [Figure 17] As one embodiment of the present invention, this is a top view illustrating feed injection region B formed on a dual flow tray when injection nozzles are provided in a form inclined at a predetermined angle on two branched inner pipes. MODE FOR CARRYING OUT THE INVENTION

[0015] Terms and words used in the description and claims of the present invention shall not be construed as being limited to their ordinary or dictionary meanings, and shall be interpreted as meanings and concepts consistent with the technical idea of the present invention in accordance with the principle that inventors can properly define the concept of terms for the purpose of describing their invention in the best mode.

[0016] With respect to the description of the drawings, similar reference numerals may be used for similar or related components.

[0017] The singular form of a noun corresponding to an item may include one or more of said items, unless the relevant context clearly indicates otherwise a different meaning.

[0018] In this disclosure, each of the phrases "A or B," "at least one of A and B," "at least one of A or B," "A, B or C," "at least one of A, B, and C," and "at least one of A, B, or C" may include any one of the items listed together with the phrase, or any possible combination thereof.

[0019] The term "and / or" includes a combination of multiple related listed components or any of the components of multiple related listed components.

[0020] Terms such as "first," "second," or "first" or "second" may be used simply to distinguish one component from others and not to limit it in any other respect (e.g., importance or order).

[0021] Furthermore, terms such as "front," "rear," "top," "bottom," "side," "left," "right," "upper," and "lower" used in this application are defined based on the drawings, and these terms do not restrict the shape and position of each component.

[0022] Terms such as “includes” or “has” indicate the presence of features, figures, steps, actions, components, parts, or combinations thereof described in this disclosure, but do not preclude the presence or possibility of adding one or more other features, figures, steps, actions, components, parts, or combinations thereof.

[0023] When one component is said to be “connected,” “joined,” “supported,” or “in contact” with another component, this includes not only cases where the components are directly connected, joined, supported, or in contact, but also cases where they are indirectly connected, joined, supported, or in contact through a third component.

[0024] When we say that one component is located "on top of" another component, this includes not only cases where one component is in contact with another, but also cases where yet another component exists between the two components.

[0025] Furthermore, the terms "approximately" and "substantially" used in this application are used either numerically or in a sense close to numerically when manufacturing and material tolerances specific to the meaning referred to are presented, and are used to facilitate understanding of the present invention and to prevent unscrupulous infringers from unfairly exploiting disclosures that refer to precise or absolute numerical values.

[0026] As used in this application, the term "stream" may mean the flow of fluid within a process, or it may mean the fluid itself flowing through piping. Specifically, the stream may simultaneously mean the fluid itself and the flow of fluid through piping connecting each device. Furthermore, the fluid may contain one or more components of gas, liquid, and solid.

[0027] In the present invention, unless otherwise specified, the "bottom of the tower" of the device means a point 95% to 100% below the top of the device, and specifically may mean the lowest point. Similarly, unless otherwise specified, the "top of the tower" of the device means a point 0% to 5% below the top of the device, and specifically may mean the highest point.

[0028] In this specification, "injection nozzle depth" means the distance between the injection nozzle 330 and the inside of the column 100 that is closest to it, and "injection nozzle height" may mean the height from the lower tray 210a to the feed supply unit 300. Also, "tray spacing (TS)" may mean the height from the lower tray 210a to the upper tray 210b at any given stage.

[0029] In the present invention, "feed injection area B" may mean the total area in which the feed injected from the injection nozzle comes into contact with the tray.

[0030] The reactive monomer separation apparatus according to the present invention will be described in detail below with reference to the drawings.

[0031] The reactive monomer separation apparatus according to the present invention is for purifying and separating highly reactive monomers such as (meth)acrylic acid, acrylic acid, methyl acrylate, or 1,3-butadiene, and more specifically, can be a vacuum distillation column. For example, reactive monomers such as acrylic acid undergo polymer formation by Michael addition reaction at high temperatures of about 100°C or higher, and have a boiling point of about 141°C at atmospheric pressure. When distillation purification is performed at atmospheric pressure, polymer formation occurs at the bottom of the distillation column, making continuous operation of the process impossible. In such cases, the purification process for reactive monomers needs to be designed as a vacuum process to lower the column temperature.

[0032] Figure 1 is a cross-sectional view of a reactive monomer separation apparatus according to one embodiment, and Figures 2 to 4 are perspective views showing an enlarged view of area A in Figure 1, and more specifically, detailed structural diagrams of the feed stage A equipped with the feed supply unit 300.

[0033] Referring to Figure 1, a separation apparatus for reactive monomers according to one embodiment of the present invention includes a cylindrical column 100.

[0034] The cylindrical column 100 is generally applicable without limitation as long as it is in a form used in a gas-liquid contact separation process, and the size of the cylindrical column 100 can be appropriately selected from the range commonly applied in the art and is not particularly limited. For example, the inner diameter of the cylindrical column 100 can be about 300 mm to 6,000 mm, more specifically about 1,500 mm to 6,000 mm, and more specifically about 1,800 mm to 4,000 mm, and the overall height of the cylindrical column 100 can be about 2,000 mm to 60,000 mm, more specifically about 5,000 mm to 50,000 mm, and more specifically about 6,000 mm to 40,000 mm, but is not limited thereto.

[0035] Furthermore, in one embodiment of the present invention, a reactive monomer separation apparatus is provided with a plurality of dual flow trays 210 inside the cylindrical column 100. Since the reactive monomer, which is the substance to be separated, polymerizes inside the column to form a polymer, there is a high risk of fouling. Therefore, in the separation apparatus according to the present invention, dual flow trays 210 are used as trays to partition the stages of the distillation column for gas-liquid separation.

[0036] The dual-float tray 210 is a sieve tray without a downcomer, and the hole 215 of the dual-float tray performs a dual function of allowing both liquid and vapor to pass through. Furthermore, because the dual-float tray has no downcomer, it offers a larger tray area, resulting in a larger capacity than conventional tray types and easier installation and maintenance. However, because the dual-float tray has no downcomer and does not redistribute the liquid, and operates with the liquid continuously flowing through the hole 215, it is less efficient, prone to channeling, and sensitive to the liquid distribution of the feed. In other words, to prevent channeling, it is necessary to add nozzles to distribute the feed uniformly, but especially in vacuum distillation columns, the manhole and flange must be minimized to maintain negative pressure inside the column, making the subsequent addition of injection nozzles difficult.

[0037] Furthermore, due to the frequent formation of polymers from the reactive monomers used as raw materials, pipe clogging occurs. As a result, complex devices commonly used in columns, such as liquid distributors, cannot be used, and the feed must be distributed as uniformly as possible onto the tray using the injection nozzle 330. Therefore, the present invention provides a reactive monomer separation apparatus that improves column separation efficiency, allows for the acquisition of high-quality products, and reduces energy consumption by designing the feed supply unit 300 to distribute the liquid phase feed as uniformly as possible, thereby preventing the channeling phenomenon that occurs in dual-float trays.

[0038] As shown in Figure 1, the plurality of dual float trays 210 can be arranged perpendicular to the height of the cylindrical column 100 and spaced apart from each other by a predetermined interval TS. The interior of the cylindrical column 100 can be divided into multiple stages 200 by the plurality of dual float trays 210.

[0039] The number and size of the dual float trays 210 are not particularly limited and can be set based on the number of theoretical stages inferred from the distillation curve considering the composition of the feedstream. In the foregoing, "number of theoretical stages" means the number of stages partitioned by a hypothetical region or tray in the separation apparatus where two phases, such as the gas phase and the liquid phase, are in equilibrium with each other.

[0040] According to one embodiment of the present invention, a feed supply unit 300 is provided in one of the plurality of stages 200, i.e., a predetermined feed stage A, so that liquid phase raw materials (feed) can be supplied into the cylindrical column 100. Here, the raw materials may include one or more reactive monomers, or mixtures containing them. For example, the reactive monomers may include, but are not limited to, (meth)acrylic acid, acrylic acid, methyl acrylate, 1,3-butadiene, or mixtures thereof.

[0041] Furthermore, the feed supply unit 300 can be positioned at a predetermined distance between the lower dual float tray 210a and the upper dual float tray 210b in a predetermined feed stage A. The height of the feed supply unit 300 can be determined according to the tray spacing TS, the column inner diameter, the injection nozzle depth, the injection angle X, and / or the feed injection direction.

[0042] For example, the height of the feed supply section 300 can be greater than 0 mm but less than TS, and more specifically, it can be between 0.25*TS and 0.75*TS. If the feed supply section 300 is positioned too low, it may be below the liquid level of the feed solution on the lower dual float tray 210a. Here, the liquid level of the solution can be calculated using a simulation program or the like. Also, if the feed supply section 300 is excessively low or high, the feed may flow down along the inner wall of the column, potentially reducing the efficiency of the column.

[0043] Referring to Figures 2 to 4, in a reactive monomer separation apparatus according to one embodiment of the present invention, the feed supply unit 300 includes a feed transfer pipe 310, an inner pipe 320, and an injection nozzle 330.

[0044] In one embodiment of the present invention, the feed transfer piping 310 can be provided in a circular shape along the inner wall of the cylindrical column 100. With the above-described structure, interference of the solution descending from the upper tray 210b to the lower tray 210a can be minimized.

[0045] In one embodiment of the present invention, the inner piping 320 is provided extending in the direction of the central axis from the circular feed transfer piping 310. More specifically, the longitudinal direction of the inner piping 320 can be provided horizontally with respect to the dual float tray 210. Furthermore, multiple inner pipes 320 can be provided; for example, the number of inner pipes can be 2 to 8, more specifically 2 to 7, and more specifically 2 to 6.

[0046] Furthermore, one or more of the internal pipes 320 can be provided at equal intervals from each other. When multiple internal pipes 320 are arranged at equal intervals from each other, the overlapping and uninjected areas of the feed injection regions B are minimized, allowing for a more uniform distribution of the feed.

[0047] In one embodiment of the present invention, the inner piping 320 can be in the form of a "straight inner piping" extending in the central axis direction from the feed transfer piping 310, as shown in Figure 2, or a "branched inner piping" including a connecting pipe 321 extending in the central axis direction from the feed transfer piping 310 and a branch pipe 322 provided at the end of the connecting pipe, as shown in Figure 3.

[0048] The branch pipe 322 can be provided perpendicular to the longitudinal direction of the connecting pipe 321 and horizontal to the dual float tray 210. The branch pipe 322 can also have a straight or curved shape. For example, when the branch pipe 322 has a curved shape, it can be provided parallel to the feed transfer pipe 310 at a predetermined interval. In addition, in a plurality of branch pipes 322, the ends of each branch pipe may be spaced equally apart without touching each other.

[0049] On the other hand, the length of the inner piping 320 with respect to the central axis can be less than 0.5 times the inner diameter of the cylindrical column 100, and more specifically, 0.1 to 0.4 times.

[0050] Specifically, if the inner piping 320 is a straight inner piping, a length must be ensured that the inner wall of the cylindrical column and two or more injection nozzles can be separated from each other at a predetermined distance. The length of the straight inner piping can be, for example, less than 0.5 times the inner diameter of the cylindrical column 100, more specifically 0.1 to 0.45 times, and more specifically 0.2 to 0.4 times.

[0051] On the other hand, if the inner piping 320 is a branched inner piping, space for the branched piping must be secured, so it is preferable that the length of the connecting piping 321 be shorter than that of a straight inner piping. For example, the length of the connecting piping 321 of the branched inner piping can be 0.4 times or less, more specifically 0.1 to 0.35 times, or more specifically 0.1 to 0.3 times, the inner diameter of the cylindrical column 100. The longer the length of the connecting piping 321, the larger the maximum radius of the feed injection region where the injected feed does not reach the inner wall of the column, and the greater the area of ​​the feed injection region.

[0052] In one embodiment of the present invention, the injection nozzle 330 is provided in the inner piping 320. Specifically, for the purpose of increasing the area of ​​the feed injection region B relative to the number of inner pipes 320, multiple injection nozzles 330 can be individually provided in each of the multiple inner pipes 320, and the multiple injection nozzles are arranged spaced apart from each other.

[0053] For example, each of the multiple inner pipes 320 may be individually equipped with two or more injection nozzles 330 per inner pipe, more specifically two to four, and more specifically two. Here, the multiple injection nozzles 330 may be provided at the end of each inner pipe 320. More specifically, the multiple injection nozzles 330 may be provided at the end and intermediate regions of each inner pipe, more specifically in the region between 1 / 3 and 2 / 3 of the total length of the inner pipe.

[0054] In one embodiment, the number of injection nozzles can correspond to the number of internal piping in a 1:2 ratio. The total number of injection nozzles can be, for example, 4 to 16, more specifically 4 to 14, and more specifically 4 to 12.

[0055] As an example, if the inner piping 320 is a straight inner piping, as shown in Figures 2 and 4, injection nozzles 330 can be provided at the end of each inner piping and between the connection point where the feed transfer piping 310 and the inner piping 320 are connected and the end of the inner piping, i.e., in the intermediate region of the inner piping. Here, the injection nozzles located in the intermediate region of the inner piping need to be spaced away from the inner wall of the column so that the injected feed does not reach the inner wall of the column. For example, Figures 6 and 7 show an embodiment in which six straight inner pipes are provided in the feed supply section. Referring to Figures 6 and 7, it can be seen that by providing two injection nozzles per inner pipe, the feed injection area B is widely and uniformly distributed on the tray.

[0056] Furthermore, if the inner piping 320 is a branched inner piping, injection nozzles 330 can be provided at both ends of the branched piping 322, as shown in Figures 3 and 5. For example, Figures 8 to 13 illustrate the number of branched inner pipes and the corresponding feed injection areas B.

[0057] Furthermore, Figures 8 and 9 show an example where the feed supply unit is equipped with two branched internal pipes, Figures 10 and 11 show an example where the feed supply unit is equipped with three branched internal pipes, and Figures 12 and 13 show an example where the feed supply unit is equipped with four branched internal pipes. Referring to Figures 8 to 13, it can be confirmed that by providing two or more injection nozzles 330 per internal pipe 320, the feed injection area B is widely and uniformly distributed on the tray.

[0058] To compare the effects of the structure of the feed supply unit 300, Figures 14 and 15 show the feed injection area B in the case where the feed supply unit can be equipped with four internal pipes, but each internal pipe is equipped with only one injection nozzle. Assuming that all conditions other than the structure of the internal pipes and the number of injection nozzles per internal pipe are the same, comparing the embodiment of the present application (Figures 12 and 13), which has the same number of internal pipes (four), with the comparative example (Figures 14 and 15), it can be confirmed that the feed injection area B of the embodiment is wider and more uniformly distributed than that of the comparative example.

[0059] On the other hand, the plurality of injection nozzles 330 can be positioned at the bottom of the inner piping 320 and configured to inject feed toward the lower dual float tray 210a, as shown in Figures 2 and 3. Alternatively, the plurality of injection nozzles 330 can be positioned at the top of the inner piping 320 and configured to inject feed toward the upper dual float tray 210b, as shown in Figures 4 and 5.

[0060] Specifically, the raw materials injected from the plurality of injection nozzles 330 form respective feed injection regions B on the lower dual float tray 210a or the upper dual float tray 210b, depending on the direction toward which the injection ports of the injection nozzles 330 face. Here, it is preferable that each of the feed injection regions B be formed with the widest possible area, but it is preferable that they do not overlap in order to ensure a uniform supply of the raw materials. Furthermore, if the feed flows down along the inner wall of the column 100, gas-liquid contact will not occur, and the separation efficiency will decrease, so the diameter of the feed injection region B must not exceed the inner diameter range of the cylindrical column 100.

[0061] On the other hand, the height of the injection nozzle 330 can be determined by the column inner diameter, tray spacing TS, injection angle X of the injection nozzle, injection nozzle depth, and / or feed injection direction, and can be the same as the height of the feed supply unit 300 described above. If the injection nozzle 330 is positioned too low, it will be below the liquid level of the feed solution on the lower dual float tray 210a, which may make it difficult to distribute the raw material over a wide area.

[0062] More specifically, if the injection nozzle 330 is located at the bottom of the inner piping 320, if the injection nozzle 330 is positioned too high, the radius of the feed injection area B becomes excessively large, causing the feed to flow down along the inner wall of the column, which can reduce the gas-liquid separation efficiency.

[0063] On the other hand, referring to Figure 16, with the injection nozzles positioned vertically to the upper or lower part of the inner piping as the baseline (0°), each of the injection nozzles 330 can also be positioned at a predetermined angle Y in the direction of the central axis of the dual float tray 210 to further expand the area of ​​the feed injection region B. Adjusting the angle of the injection nozzles may be even more effective when branched inner piping is provided, in terms of expanding the area of ​​the feed injection region B and preventing overlap between the feed injection regions B.

[0064] Figures 16 and 17 illustrate an example of a feed injection area B in which an injection nozzle is provided in the feed supply section at a predetermined angle Y. Generally, to enlarge the area of ​​the feed injection area B, an injection nozzle with a large injection angle X must be used, or the injection nozzle must be positioned higher. However, the injection angle X of the injection nozzle is fixed by the product and difficult to change, and there are product limitations. Furthermore, there are limitations to adjusting the height of the injection nozzle due to the tray spacing. Thus, when it is difficult to change conditions such as the injection angle X and height of the injection nozzle, the area of ​​the feed injection area B can be increased, as shown in Figure 17, by adjusting the installation angle Y of the injection nozzle, as shown in Figure 16.

[0065] Furthermore, in the case of upward injection as illustrated in Figures 4 and 5, if the distance between the injection nozzle 330 and the upper tray 210b is too great, the feed may not contact the upper tray and may fall in a parabolic trajectory. Therefore, when the injection nozzle is located at the top of the internal piping, adjusting the angle of the injection nozzle may be effective when the distance from the upper tray to the nozzle is less than the height of the injection nozzle.

[0066] More specifically, if the injection nozzle 330 is provided in an inclined position in the direction of the central axis, there is an advantage in that even if it is shorter than the length of the inner piping (or connecting piping), or if the injection angle X is large, or if the injection nozzle is installed at a high position, the risk of the feed contacting the inner wall of the column can be prevented. However, if the feed injected from the injection nozzle 330 is injected parallel to the tray 210, the feed can be injected onto the inner wall of the column on the opposite side of the inner piping where the injection nozzle is located, and it is preferable that the installation angle Y of the injection nozzle satisfies the following relational expression 1.

[0067] [Relationship 1] 0.5X + Y < 90

[0068] In the above relational equation 1, X is the injection angle of the injection nozzle, and Y is the angle of inclination relative to the time when the injection nozzle is mounted perpendicular to the inner piping (see Figure 16).

[0069] More specifically, even if the feed is injected over an area that is too wide relative to the inner diameter of the column, the feed can be injected into the inner wall of the column on the opposite side of the inner piping where the injection nozzle is located, and it is more preferable that the installation angle Y of the injection nozzle also satisfies the following relational equation 2.

[0070] [Relationship 2] tan(0.5X+Y)<(Dl) / h

[0071] In relational equation 2 above, X is the injection angle of the injection nozzle, Y is the angle of inclination relative to the time when the injection nozzle is mounted perpendicular to the inner piping (see Figure 16), D is the inner diameter of the column, l is the depth of the injection nozzle, and h is the height of the injection nozzle.

[0072] As an example, a theoretical calculation of the change in the area of ​​the feed injection region due to the injection angle X and the installation angle Y of the injection nozzle yields the results shown in Table 1 below. Specifically, Table 1 below assumes that the area of ​​the feed injection region is 1 when the injection angle X of the injection nozzle is 90° and the injection nozzle is positioned perpendicular to the inner piping (Y=0°) and the feed is injected, and calculates and summarizes the ratio of the relative area due to the change in the injection angle X and the installation angle Y of the injection nozzle.

[0073] [Table 1]

[0074] Referring to Table 1 above, for example, if the nozzle's spray angle X is 30° and the nozzle's installation angle Y is set to 60°, the area of ​​the feed spray region B theoretically increases by approximately 10 times. If the nozzle's spray angle X is 150° and the nozzle's installation angle Y is set to 10°, the area of ​​the feed spray region B theoretically increases by approximately 1.85 times. Therefore, the smaller the nozzle's spray angle X, the greater the relative increase in the feed spray region area when the nozzle's installation angle Y is adjusted.

[0075] On the other hand, a separation apparatus according to one embodiment of the present invention may further include a lower outlet 400 provided at the bottom of the cylindrical column 100 for discharging a liquid phase stream, and an upper outlet 500 provided at the top of the cylindrical column for discharging a gas phase stream.

[0076] The raw materials supplied into the cylindrical column 100 undergo a separation process through continuous gas-liquid contact at each stage of the column. The relatively lighter components, which are low-boiling point components, rise in vapor form and are discharged through the upper outlet 500 at the top of the column, while the relatively heavier components, which are high-boiling point components, descend as a condensed liquid phase and are discharged through the lower outlet 400 at the bottom of the column. For example, if a feed containing acrylic acid is supplied, the acrylic acid can be discharged through the lower outlet 400, but is not limited to this.

[0077] In each stage of the dual float tray 210, the rising gas phase stream at the top and the descending liquid phase stream at the bottom come into contact with each other, transferring heat and mass. As a result, some of the high-boiling-point components condense and flow down to the bottom, while the uncondensed vapor continues to rise to the top, a continuous process.

[0078] Although the reactive monomer separation apparatus according to the present invention has been described and illustrated in the drawings above, the description and illustrations above only describe and illustrate the core components necessary for understanding the present invention. In addition to the processes and apparatus described and illustrated above, processes and apparatus not described and illustrated elsewhere can be appropriately applied and used to carry out the reactive monomer separation apparatus according to the present invention.

[0079] While exemplary embodiments of the present invention have been described above, the present invention is not limited thereto, and a person with ordinary skill in the art will understand that various modifications and variations are possible without departing from the concepts and scope of the claims described below. [Explanation of Symbols]

[0080] 100 cylindrical columns 200 stages 210 Dual Float Tray 215 holes 300 Feed supply unit 310 Feed transfer piping 320 Internal piping 330 spray nozzles 321 Connecting piping 322 Branch piping 400 Lower outlet 500 Upper outlet

Claims

1. A cylindrical column and The cylindrical column is provided with multiple dual float trays that divide multiple stages, It includes a feed supply unit provided in one of the aforementioned plurality of stages, which supplies a raw material containing a liquid-phase reactive monomer, The aforementioned feed supply unit is A circular feed transfer pipe is provided along the inner wall of the cylindrical column, spaced apart between the lower dual float tray and the upper dual float tray of the stage where the feed supply unit is located, Multiple internal pipes extending in the central axis direction from the aforementioned feed transfer pipe, This includes a plurality of injection nozzles provided in the plurality of inner pipes, A separation apparatus for reactive monomers, wherein each of the aforementioned multiple internal pipes is individually equipped with multiple injection nozzles.

2. The aforementioned internal piping is A connecting pipe extending in the central axis direction from the aforementioned feed transfer pipe, The reactive monomer separation apparatus according to claim 1, further comprising a branch pipe provided at the end of the connecting pipe.

3. The reactive monomer separation apparatus according to claim 2, wherein the branch piping is provided in one form selected from straight lines and curves.

4. The reactive monomer separation apparatus according to claim 2, wherein injection nozzles are provided at both ends of the branched pipe.

5. The reactive monomer separation apparatus according to claim 1, wherein each of the injection nozzles is provided in a state inclined at a predetermined angle in the direction of the central axis.

6. The reactive monomer separation apparatus according to claim 1, wherein the plurality of injection nozzles are provided to inject raw materials toward the upper dual float tray.

7. The reactive monomer separation apparatus according to claim 1, wherein the number of internal pipes is 2 to 8.

8. The separation apparatus for reactive monomers according to claim 1, wherein the plurality of internal pipes are spaced equally apart from one another.

9. The apparatus for separating reactive monomers according to claim 1, wherein the reactive monomer comprises (meth)acrylic acid, acrylic acid, methyl acrylate, 1,3-butadiene, or a mixture thereof.

10. The separation apparatus for reactive monomers according to claim 1, wherein the separation apparatus is a vacuum distillation column.

11. A lower outlet is provided at the bottom of the cylindrical column for discharging the liquid phase stream, The reactive monomer separation apparatus according to claim 1, further comprising an upper outlet provided at the top of the cylindrical column for discharging a gas phase stream.

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