A butyraldehyde condensation reaction system

Abstract

The utility model provides a kind of butyl aldehyde condensation reaction system, which comprises: lye feed line, stripping nitrogen pipeline, n-butyl aldehyde feed line, lye oxygen removal tower and condensation reactor;The bottom outlet of the lye oxygen removal tower is connected to the condensation reactor;The lye feed line and the stripping nitrogen pipeline are both connected to the lye oxygen removal tower, and the lye feed line is located above the stripping nitrogen pipeline;The n-butyl aldehyde feed line is connected to the side wall of the condensation reactor;The material outlet of the condensation reactor is connected to a discharge line.This butyl aldehyde condensation reaction system can effectively inhibit the occurrence of side reactions and improve the conversion rate of raw materials.

Description

Technical Field

[0001] This utility model relates to the field of condensation reaction technology, and more specifically, to a butyraldehyde condensation reaction system. Background Technology

[0002] Butanol and octanol are important raw materials for the synthesis of fine chemical products. Currently, my country's butanol and octanol production is enormous, accounting for approximately 21% of the world's total. Butanol and octanol are mainly used in the production of plasticizers, solvents, dehydrating agents, defoamers, dispersants, flotation agents, petroleum additives, and synthetic fragrances. Due to their wide range of applications, the production and consumption of butanol and octanol have been increasing year by year. Butanol and octanol are usually prepared through the condensation of n-butyraldehyde. Specifically, n-butyraldehyde undergoes condensation and dehydration under the catalysis of sodium hydroxide to produce octenal. Octenal is then hydrogenated to produce crude octanol, which is then distilled to obtain the final product, butanol and octanol.

[0003] In related technologies, the sodium hydroxide solution used in the butyraldehyde condensation process is typically prepared by adding a 25-50 wt% sodium hydroxide solution directly to the condensation reactor after preparation in a storage tank. However, the sodium hydroxide solution added directly to the condensation reactor carries some oxygen. The addition of this oxygen can lead to side reactions during the condensation process, producing butyric acid and butyrate, which affects the product yield. Furthermore, these byproducts can corrode the condensation reactor, affecting its service life.

[0004] In view of the above, this utility model is hereby proposed. Utility Model Content

[0005] The purpose of this invention is to provide a butyraldehyde condensation reaction system. This system can effectively reduce side reactions during the condensation process by pre-deoxygenating the alkaline solution, thereby improving the utilization rate of the raw material n-butyraldehyde, reducing catalyst consumption, reducing the formation of sodium salts in wastewater, and reducing the corrosion of equipment and pipelines by the byproduct butyric acid. This helps to reduce production and operating costs.

[0006] In order to achieve the above-mentioned objectives of this utility model, the following technical solution is adopted: This invention provides a butyraldehyde condensation reaction system, comprising: an alkali feed pipeline, a stripping nitrogen pipeline, a n-butyraldehyde feed pipeline, an alkali deoxygenation tower, and a condensation reactor; the bottom outlet of the alkali deoxygenation tower is connected to the condensation reactor; both the alkali feed pipeline and the stripping nitrogen pipeline are connected to the alkali deoxygenation tower, and the alkali feed pipeline is located above the stripping nitrogen pipeline; the n-butyraldehyde feed pipeline is connected to the side wall of the condensation reactor; and the material outlet of the condensation reactor is connected to a discharge pipeline.

[0007] In the above technical solution, by introducing nitrogen gas into the alkaline deoxygenation tower, the oxygen contained in the alkaline solution can be stripped by nitrogen gas, thereby effectively reducing the oxygen carried in the alkaline solution, reducing side reactions during the condensation process (mainly reducing the oxidation of n-butyraldehyde to produce butyric acid as a byproduct), improving the utilization rate of the raw material n-butyraldehyde, reducing catalyst consumption, and reducing the formation of sodium salts (generated by the reaction of butyric acid and alkaline solution) in the wastewater. At the same time, with the reduction of side reactions, the byproduct butyric acid can be significantly reduced, which helps to reduce corrosion of equipment, pipelines, etc., and reduce production and operating costs.

[0008] For example, the alkaline deoxygenation tower is equipped with a disperser, which is located vertically above the stripping nitrogen pipeline, and the alkaline feed pipeline is connected to the disperser.

[0009] In the above technical solution, the alkaline solution is sprayed into the alkaline deoxygenation tower via a disperser. This solution, by spraying the alkaline solution from top to bottom, increases the contact area between the alkaline solution and nitrogen gas, improves the stripping deoxygenation efficiency, and thus further reduces the amount of oxygen in the alkaline solution.

[0010] For example, it also includes an alkali solution preparer and an alkali solution intermediate tank. The bottom of the alkali solution preparer is connected to the alkali solution intermediate tank, and the inlet of the alkali solution feed pipe is connected to the bottom of the alkali solution intermediate tank. The top of the alkali solution intermediate tank is connected to a first nitrogen-sealing pipeline, and nitrogen enters the alkali solution intermediate tank through the first nitrogen-sealing pipeline.

[0011] In this example, by using a first nitrogen-sealing pipeline to seal the intermediate alkaline tank, it is ensured that oxygen in the air cannot enter, thus preventing oxygen from being carried into the subsequent condensation reaction by the alkaline solution. This helps to reduce side reactions during the condensation process and improve the utilization rate of raw materials and the yield of products.

[0012] For example, the top of the condensation reactor is connected to a second nitrogen-sealing pipeline, through which nitrogen enters the condensation reactor.

[0013] In this example, by setting up a second nitrogen-sealing pipeline, it can be ensured that oxygen in the air cannot enter during the condensation reaction, thus avoiding side reactions caused by oxygen entry and improving the raw material conversion rate.

[0014] For example, the condensation reaction tower includes a pre-reaction section and a deep reaction section, the deep reaction section being located above the pre-reaction section, and the bottom outlet of the alkali deoxygenation tower being connected to the pre-reaction section and the deep reaction section respectively; a circulation pipeline is connected to the bottom of the pre-reaction section, and the outlet of the circulation pipeline is connected to the side wall of the pre-reaction section and the side wall of the deep reaction section respectively, and the discharge pipeline is located on the side wall of the deep reaction section.

[0015] The above scheme, by dividing the condensation reaction tower into two reaction sections, allows the raw materials to undergo two reactions, which helps to improve the conversion rate of the raw materials.

[0016] For example, an enhanced reaction unit is provided in the pre-reaction section, and the bottom outlet of the alkali deoxygenation tower is connected to the enhanced reaction unit through the side wall of the pre-reaction section.

[0017] In this example, the alkali solution can be dispersed and broken into micron-sized droplets by an enhanced reaction unit. This helps to improve the uniformity of the alkali solution distribution in n-butyraldehyde, increase the phase boundary mass transfer area, and significantly improve the mass transfer rate, thereby helping to improve the reaction efficiency of raw materials and the yield of products.

[0018] For example, the enhanced reaction unit includes a first enhanced mass transfer reactor and a second enhanced mass transfer reactor, with the first enhanced mass transfer reactor located above the second enhanced mass transfer reactor; the bottom outlet of the alkali deoxygenation tower is connected to the first enhanced mass transfer reactor and the second enhanced mass transfer reactor respectively; the outlets of the first enhanced mass transfer reactor and the second enhanced mass transfer reactor are opposite to each other, and the outlet of the n-butyraldehyde feed pipeline is located between the first enhanced mass transfer reactor and the second enhanced mass transfer reactor.

[0019] In this scheme, by positioning the outlets of the two enhanced mass transfer reactors opposite each other, the opposing forces between the two microdroplets can further disperse and break them up, allowing them to be rapidly dispersed into the n-butyraldehyde, thus improving the uniformity of the alkali solution distribution within the n-butyraldehyde. By placing the outlet of the n-butyraldehyde feed pipe between the two enhanced mass transfer reactors, the n-butyraldehyde feed impacts the microdroplets between the reactors, causing them to redistribute and further improving the uniformity of the microdroplet distribution within the n-butyraldehyde. Simultaneously, it allows for rapid mixing of the n-butyraldehyde and the alkali solution, further increasing the contact area between the two phases, enhancing mass transfer, and accelerating the reaction process.

[0020] For example, the outlets of the first enhanced mass transfer reactor and the second enhanced mass transfer reactor are connected by an enhanced dispersion tube, and the enhanced dispersion tube is provided with a plurality of dispersion ports on the side facing the outlet of the n-butyraldehyde feed pipeline.

[0021] In the above scheme, by setting up an enhanced dispersion tube, the microdroplet collision process between the two enhanced mass transfer reactors can be separated from the redistribution process of the n-butyraldehyde feed impact. Specifically, the microdroplets generated by each of the two enhanced mass transfer reactors first undergo collision in the enhanced dispersion tube for further dispersion and breakage, and then impact and rapidly mix with the n-butyraldehyde feed through the dispersion port. This helps to further improve the uniformity of the alkali solution distribution in n-butyraldehyde and the phase interface contact area between n-butyraldehyde and the alkali solution.

[0022] For example, a distributor is provided in the pre-reaction section, and the outlet of the n-butyraldehyde feed pipeline is connected to the distributor. The outlet of the distributor faces the region between the first enhanced mass transfer reactor and the second enhanced mass transfer reactor. The distributor may have orifices with different orientations.

[0023] In the above scheme, the n-butyraldehyde feed is injected in different directions via a distributor, causing the microdroplets between the two enhanced mass transfer reactors to distribute rapidly and evenly. This further improves the uniformity of the distribution of the alkali solution in the n-butyraldehyde.

[0024] For example, a third enhanced mass transfer reactor is provided in the deep reaction section; the bottom outlet of the alkali deoxygenation tower is connected to the third enhanced mass transfer reactor, the outlet of the third enhanced mass transfer reactor is downward, and a distribution plate is provided at the outlet of the third enhanced mass transfer reactor.

[0025] The above scheme, by setting up a third enhanced mass transfer reactor, can disperse and break the alkali solution into micro-droplets, and then use a distribution disk to quickly and evenly distribute them into the n-butyraldehyde in the deep reaction section. This helps to increase the phase interface contact area between the alkali solution and n-butyraldehyde in the deep reaction section and improve the reaction efficiency.

[0026] It will be understood by those skilled in the art that the enhanced mass transfer reactor used in this utility model has been reflected in the inventor's prior patents, such as patents with application numbers CN201610641119.6, CN201610641251.7, CN201710766435.0, CN106187660A, CN105903425A, CN205833127U and CN207581700U. The prior patent CN201610641119.6 details the specific product structure and working principle of a micron-sized bubble generator (i.e., a bubble breaker). This application document states that "the micron-sized bubble generator includes a main body and a secondary breaking component. The main body has a cavity, and an inlet communicating with the cavity is provided on the main body. The first and second ends of the cavity are both open, and the cross-sectional area of ​​the cavity decreases from the middle of the cavity towards the first and second ends. The secondary breaking component is located at at least one of the first and second ends of the cavity, with a portion of the secondary breaking component located within the cavity. A ring-shaped channel is formed between the secondary breaking component and the open through-holes at both ends of the cavity. The micron-sized bubble generator also includes an air inlet pipe and a liquid inlet pipe." From the specific structure disclosed in this application document, its specific working principle can be understood as follows: liquid enters the micron-sized bubble generator tangentially through the liquid inlet pipe, rotates at ultra-high speed, and cuts the gas, causing the gas bubbles to break into micron-sized microbubbles, thereby increasing the mass transfer area between the liquid and gas phases. Moreover, the micron-sized bubble generator in this patent is a pneumatic bubble breaker.

[0027] Furthermore, prior patent 201610641251.7 describes a primary bubble breaker with a circulating liquid inlet, a circulating gas inlet, and a gas-liquid mixture outlet, while a secondary bubble breaker connects the feed inlet to the gas-liquid mixture outlet. This indicates that both bubble breakers require a gas-liquid mixture to enter. Additionally, as shown in the accompanying drawings, the primary bubble breaker primarily utilizes the circulating liquid as its power source, thus classifying it as a hydraulically driven enhanced reactor. The secondary bubble breaker simultaneously introduces the gas-liquid mixture into an elliptical rotating sphere for rotation, thereby achieving bubble breakage during rotation. Therefore, the secondary bubble breaker is actually a gas-liquid linked bubble breaker. In fact, both hydraulically driven and gas-liquid linked bubble breakers are specific forms of bubble breakers. However, the enhanced mass transfer unit used in this invention is not limited to these forms; the specific structure of the bubble breaker described in the prior patent is merely one possible form for this invention.

[0028] Furthermore, prior patent 201710766435.0 states that "the principle of the bubble breaker is to achieve mutual collision of gases by high-speed jetting"; and prior patent CN106187660 also describes the specific structure of the bubble breaker, as detailed in paragraphs

[0031] -

[0041] of the specification and the attached drawings. It elaborates on the specific working principle of the bubble breaker S-2. The top of the bubble breaker is the liquid phase inlet, and the side is the gas phase inlet. The liquid phase entering from the top provides the entrainment force, thereby achieving the effect of crushing into ultrafine bubbles. The attached drawings also show that the bubble breaker has a conical structure, with the upper diameter being larger than the lower diameter, which is also to allow the liquid phase to provide better entrainment force.

[0029] Because bubble breakers were newly developed in the early stages of the prior patent application, they were initially named micron bubble generators (CN201610641119.6), etc. With continuous technological improvements, the name was later changed to bubble breaker. The enhanced mass transfer unit in this utility model is equivalent to the previous micron bubble generator, micro-interface generator, etc., only with different names. In summary, the enhanced mass transfer reactor of this utility model belongs to the prior art.

[0030] Compared with the prior art, the beneficial effects of this utility model are as follows: The above technical solution introduces nitrogen gas into the alkaline deoxygenation tower, which can strip the oxygen contained in the alkaline solution, thereby effectively reducing the oxygen carried in the alkaline solution, reducing side reactions during the condensation process (mainly reducing the oxidation of n-butyraldehyde to produce butyric acid as a byproduct), improving the utilization rate of the raw material n-butyraldehyde, reducing catalyst consumption, and reducing the formation of sodium salts (generated by the reaction of butyric acid and alkaline solution) in the wastewater. At the same time, with the reduction of side reactions, the byproduct butyric acid can be significantly reduced, which helps to reduce corrosion of equipment, pipelines, etc., and reduce production and operating costs. Attached Figure Description

[0031] Various other advantages and benefits will become apparent to those skilled in the art upon reading the following detailed description of preferred embodiments. The accompanying drawings are for illustrative purposes only and are not intended to limit the scope of the invention. Furthermore, the same reference numerals denote the same parts throughout the drawings. In the drawings: Figure 1 A schematic diagram of the system of Embodiment 1 of this utility model is shown.

[0032] In the diagram: 1. Alkali solution preparer; 2. Heat exchanger; 3. Alkali intermediate tank; 4. First nitrogen-sealing pipeline; 5. Alkali deoxygenation tower; 6. Deep reaction section; 7. Distribution plate; 8. Third enhanced mass transfer reactor; 9. Pre-reaction section; 10. First enhanced mass transfer reactor; 11. Enhanced dispersion pipe; 12. Second enhanced mass transfer reactor; 13. Circulating alkali solution inlet; 14. Butyraldehyde feed pipeline; 15. Circulation pipeline; 16. Distributor; 17. Dispersion port; 18. Second nitrogen-sealing pipeline; 19. Discharge pipeline; 20. Alkali solution feed pipeline; 21. Disperser; 22. Stripping nitrogen pipeline. Detailed Implementation

[0033] The technical solution of this utility model will be clearly and completely described below with reference to the accompanying drawings and specific embodiments. However, those skilled in the art will understand that the embodiments described below are only some embodiments of this utility model, not all embodiments, and are only used to illustrate this utility model, and should not be regarded as limiting the scope of this utility model. Based on the embodiments of this utility model, all other embodiments obtained by those skilled in the art without creative effort are within the protection scope of this utility model. Where specific conditions are not specified in the embodiments, conventional conditions or conditions recommended by the manufacturer shall be followed. Where the manufacturers of reagents or instruments are not specified, they are all conventional products that can be purchased commercially.

[0034] In the description of this utility model, it should be noted that the terms "center," "upper," "lower," "left," "right," "vertical," "horizontal," "inner," and "outer," etc., indicating the orientation or positional relationship, are based on the orientation or positional relationship shown in the accompanying drawings and are only for the convenience of describing this utility model and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation, and therefore should not be construed as a limitation of this utility model. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and should not be construed as indicating or implying relative importance.

[0035] In the description of this utility model, it should be noted that, unless otherwise explicitly specified and limited, the terms "installation," "connection," and "joining" should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral connection; they can refer to a mechanical connection or an electrical connection; they can refer to a direct connection or an indirect connection through an intermediate medium; and they can refer to the internal connection of two components. Those skilled in the art can understand the specific meaning of the above terms in this utility model based on the specific circumstances.

[0036] To more clearly illustrate the technical solution of this utility model, the following description is provided in the form of specific embodiments.

[0037] Example 1 See Figure 1 The butyraldehyde condensation reaction system includes: an alkali feed pipeline 20, a stripping nitrogen pipeline 22, a n-butyraldehyde feed pipeline 14, an alkali deoxygenation tower 5, and a condensation reactor; the bottom outlet of the alkali deoxygenation tower 5 is connected to the condensation reactor; both the alkali feed pipeline 20 and the stripping nitrogen pipeline 22 are connected to the alkali deoxygenation tower 5, and the alkali feed pipeline 20 is located above the stripping nitrogen pipeline 22; the n-butyraldehyde feed pipeline 14 is connected to the side wall of the condensation reactor; the material outlet of the condensation reactor is connected to a discharge pipeline 19.

[0038] In this embodiment, the system also includes a circulating alkali inlet 13, which can be used to reintroduce the alkali recovered during subsequent product purification into the condensation reactor to continue participating in the reaction. In this embodiment, the circulating alkali inlet 13 is connected to the pipeline between the alkali deoxygenation tower 5 and the condensation reactor.

[0039] Continue reading Figure 1 The alkaline deoxygenation tower 5 is equipped with a disperser 21, which is located vertically above the stripping nitrogen pipeline 22. The alkaline feed pipeline 20 is connected to the disperser 21.

[0040] In this embodiment, the system also includes an alkali solution preparer 1 and an alkali solution intermediate tank 3. The bottom of the alkali solution preparer 1 is connected to the alkali solution intermediate tank 3, and the inlet of the alkali solution feed pipe 20 is connected to the bottom of the alkali solution intermediate tank 3. The top of the alkali solution intermediate tank 3 is connected to a first nitrogen sealing pipeline 4, and nitrogen enters the alkali solution intermediate tank 3 through the first nitrogen sealing pipeline 4.

[0041] In this embodiment, the discharge pipe 19 passes through the alkali solution preparer 1 and is thermally coupled to the stripping nitrogen pipe 22 via a heat exchanger 2. This allows the octenal, which has a higher temperature in the discharge pipe, to heat the alkali solution in the alkali solution preparer 1 and the nitrogen in the stripping nitrogen pipe 22. This method of fully utilizing the waste heat from the discharge helps reduce production costs and improve energy efficiency.

[0042] To further prevent the entry of external oxygen, a second nitrogen sealing pipeline 18 is connected to the top of the condensation reactor, through which nitrogen enters the condensation reactor.

[0043] Continue reading Figure 1 The condensation reaction tower includes a pre-reaction section 9 and a deep reaction section 6. The deep reaction section 6 is located above the pre-reaction section 9. The bottom outlet of the alkaline deoxygenation tower 5 is connected to the pre-reaction section 9 and the deep reaction section 6 respectively. The bottom of the pre-reaction section 9 is connected to a circulation pipeline 15. The outlet of the circulation pipeline 15 is connected to the side wall of the pre-reaction section 9 and the side wall of the deep reaction section 6 respectively. The discharge pipeline 19 is located on the side wall of the deep reaction section 6.

[0044] The pre-reaction section 9 is equipped with an enhanced reaction unit, and the bottom outlet of the alkali deoxygenation tower 5 passes through the side wall of the pre-reaction section 9 and connects to the enhanced reaction unit. The enhanced reaction unit includes a first enhanced mass transfer reactor 10 and a second enhanced mass transfer reactor 12, with the first enhanced mass transfer reactor 10 located above the second enhanced mass transfer reactor 12. The bottom outlet of the alkali deoxygenation tower 5 is connected to both the first enhanced mass transfer reactor 10 and the second enhanced mass transfer reactor 12. The outlets of the first enhanced mass transfer reactor 10 and the second enhanced mass transfer reactor 12 are opposite each other, and the outlet of the butyraldehyde feed pipeline 14 is located between the first enhanced mass transfer reactor 10 and the second enhanced mass transfer reactor 12.

[0045] In this embodiment, the outlets of the first enhanced mass transfer reactor 10 and the second enhanced mass transfer reactor 12 are connected by an enhanced dispersion pipe 11. The enhanced dispersion pipe 11 has multiple dispersion ports 17 on the side facing the outlet of the n-butyraldehyde feed pipe 14. A distributor 16 is provided in the pre-reaction section 9, and the outlet of the n-butyraldehyde feed pipe 14 is connected to the distributor 16. The outlet of the distributor 16 faces the area between the first enhanced mass transfer reactor 10 and the second enhanced mass transfer reactor 12. The distributor may have orifices with different orientations.

[0046] Continue reading Figure 1The deep reaction section 6 is equipped with a third enhanced mass transfer reactor 8; the bottom outlet of the alkaline deoxygenation tower 5 is connected to the third enhanced mass transfer reactor 8, the outlet of the third enhanced mass transfer reactor 8 is downward, and a distribution plate 7 is installed at the outlet of the third enhanced mass transfer reactor 8.

[0047] It is understandable that pumps can be installed on pipelines as needed to facilitate the flow of materials, which will not be elaborated further.

[0048] In one specific implementation of this embodiment, qualified sodium hydroxide solid (purchased externally) and pure water produced by a pure water unit are first dissolved in an alkali solution preparer to prepare a sodium hydroxide solution with specifications of 25-50%wt and a temperature of 25-80℃. The prepared alkali solution is then transported to an intermediate alkali solution tank. The alkali solution from the intermediate tank is then fed into an alkali solution deoxygenation tower via an alkali solution feed pipeline for deoxygenation. The operating pressure inside the alkali solution deoxygenation tower is 0.2-0.7MPa, and the operating temperature is 25-80℃. The deoxygenated alkali solution flows out from the bottom of the alkali solution deoxygenation tower, and testing shows that the oxygen content carried in the alkali solution is less than 1ppm. The stripped nitrogen gas is discharged from the top and enters the tail gas treatment system. The deoxygenated alkali solution is then sent to a condensation reactor to catalyze the reaction of n-butyraldehyde to produce octenal, and the product octenal is output via a discharge pipeline.

[0049] The conversion rate of n-butyraldehyde was tested to be 99.38%.

[0050] Comparative Example 1 The difference between this embodiment and Embodiment 1 is that the prepared alkali solution is directly fed into the condensation reactor.

[0051] The conversion rate of n-butyraldehyde was tested to be 88.72%.

[0052] Comparing Example 1 with Comparative Example 1, it can be found that the n-butyraldehyde conversion rate of Example 1 is significantly higher than that of Comparative Example 1. This indicates that the present invention effectively inhibits the occurrence of side reactions during the reaction process and improves the raw material conversion rate by deoxygenating the alkaline solution.

[0053] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of this utility model, and are not intended to limit it. Although the utility model has been described in detail with reference to the foregoing embodiments, those skilled in the art should understand that modifications can still be made to the technical solutions described in the foregoing embodiments, or equivalent substitutions can be made to some or all of the technical features therein. Such modifications or substitutions do not cause the essence of the corresponding technical solutions to deviate from the scope of the technical solutions of the embodiments of this utility model.

Claims

1. A butyraldehyde condensation reaction system, characterized in that, include: The system includes an alkali feed pipeline, a stripping nitrogen pipeline, a butyraldehyde feed pipeline, an alkali deoxygenation tower, and a condensation reactor; the bottom outlet of the alkali deoxygenation tower is connected to the condensation reactor. Both the alkali feed pipeline and the stripping nitrogen pipeline are connected to the alkali deoxygenation tower, and the alkali feed pipeline is located above the stripping nitrogen pipeline; The butyraldehyde feed line is connected to the side wall of the condensation reactor; the material outlet of the condensation reactor is connected to a discharge line.

2. The system according to claim 1, characterized in that, The alkaline deoxygenation tower is equipped with a disperser, which is located vertically above the stripping nitrogen pipeline, and the alkaline feed pipeline is connected to the disperser.

3. The system according to claim 1, characterized in that, It also includes an alkali solution preparer and an alkali solution intermediate tank. The bottom of the alkali solution preparer is connected to the alkali solution intermediate tank, and the inlet of the alkali solution feed pipe is connected to the bottom of the alkali solution intermediate tank. The top of the alkali solution intermediate tank is connected to a first nitrogen-sealing pipeline, and nitrogen enters the alkali solution intermediate tank through the first nitrogen-sealing pipeline.

4. The system according to claim 1, characterized in that, The top of the condensation reactor is connected to a second nitrogen-sealing pipeline, through which nitrogen enters the condensation reactor.

5. The system according to any one of claims 1-4, characterized in that, The condensation reaction tower includes a pre-reaction section and a deep reaction section, with the deep reaction section located above the pre-reaction section. The bottom outlet of the alkali deoxygenation tower is connected to both the pre-reaction section and the deep reaction section. A circulation pipeline is connected to the bottom of the pre-reaction section, and the outlet of the circulation pipeline is connected to both the side wall of the pre-reaction section and the side wall of the deep reaction section. The discharge pipeline is located on the side wall of the deep reaction section.

6. The system according to claim 5, characterized in that, An enhanced reaction unit is installed in the pre-reaction section, and the bottom outlet of the alkali deoxygenation tower is connected to the enhanced reaction unit through the side wall of the pre-reaction section.

7. The system according to claim 6, characterized in that, The enhanced reaction unit includes a first enhanced mass transfer reactor and a second enhanced mass transfer reactor, with the first enhanced mass transfer reactor located above the second enhanced mass transfer reactor; the bottom outlet of the alkali deoxygenation tower is connected to both the first enhanced mass transfer reactor and the second enhanced mass transfer reactor; the outlets of the first enhanced mass transfer reactor and the second enhanced mass transfer reactor are opposite each other, and the outlet of the n-butyraldehyde feed pipeline is located between the first enhanced mass transfer reactor and the second enhanced mass transfer reactor.

8. The system according to claim 7, characterized in that, The outlets of the first enhanced mass transfer reactor and the second enhanced mass transfer reactor are connected by an enhanced dispersion pipe, and the enhanced dispersion pipe is provided with multiple dispersion ports on the side facing the outlet of the n-butyraldehyde feed pipe.

9. The system according to claim 7, characterized in that, A distributor is provided in the pre-reaction section, and the outlet of the n-butyraldehyde feed pipeline is connected to the distributor. The outlet of the distributor faces the area between the first enhanced mass transfer reactor and the second enhanced mass transfer reactor.

10. The system according to claim 5, characterized in that, A third enhanced mass transfer reactor is provided within the deep reaction section; the bottom outlet of the alkali deoxygenation tower is connected to the third enhanced mass transfer reactor, the outlet of the third enhanced mass transfer reactor faces downward, and a distribution plate is provided at the outlet of the third enhanced mass transfer reactor.

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