n-butyraldehyde condensation reaction liquid separation system and n-butyraldehyde condensation reaction system

Abstract

The utility model provides a kind of n-butyraldehyde condensation reaction liquid separation system and n-butyraldehyde condensation reaction system, this n-butyraldehyde condensation reaction liquid separation system includes: condensation reaction liquid pipeline, heat exchanger, condenser, octene aldehyde pipeline and oil-water separator;Condensation reaction liquid pipeline is heat exchanged with octene aldehyde pipeline through heat exchanger, and after condensation through condenser, it enters oil-water separator through the separation inlet of oil-water separator;Oil-water separator side is provided with separation inlet, and other side is provided with product outlet, and product outlet is connected with the inlet of octene aldehyde pipeline;Inner piece coalescence wire net and baffle are provided in oil-water separator, and inner piece coalescence wire net and baffle are sequentially arranged between separation inlet and product outlet;Baffle is vertically arranged and baffle top has interval between oil-water separator top;Oil-water separator bottom is provided with separation zone water bag and oil collection area water bag, and separation zone water bag is located between inner piece coalescence wire net and baffle.The system can effectively reduce the water content of octene aldehyde.

Description

Technical Field

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

[0002] The self-condensation of n-butyraldehyde to octenal in the presence of sodium hydroxide is a key step in the industrial production of octanol. Octanol is an important raw material for the synthesis of fine chemical products and is mainly used in the production of plasticizers, solvents, surfactants, lubricant additives, and in the synthesis of pharmaceuticals and fragrances.

[0003] Butyraldehyde undergoes condensation and dehydration under the catalysis of sodium hydroxide to produce octenal. The aqueous and organic phases of octenal are then separated using a water-oil two-phase separator. Most of the separated aqueous phase is returned to the condensation reactor after supplementation with sodium hydroxide solution, serving as a catalyst for the butyraldehyde condensation reaction. A small amount of aqueous phase is discharged as wastewater from the condensation unit. This wastewater is typically highly alkaline and, due to the presence of a small amount of organic phase, has a high COD, making it difficult to treat. The separated organic phase of octenal is hydrogenated to produce crude octanol, which is then distilled to obtain the final product, octanol. However, this process often involves a small amount of water entrained in the organic phase of octenal, leading to high energy consumption in subsequent octenal hydrogenation and affecting the lifespan of the hydrogenation catalyst.

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

[0005] The primary objective of this invention is to provide a separation system for the n-butyraldehyde condensation reaction liquid. This system can efficiently separate the aqueous and oil phases in the n-butyraldehyde condensation product, improving the purity and yield of octenal and reducing the water entrainment in octenal. This helps reduce the energy consumption of subsequent octenal hydrogenation and minimizes the impact on the hydrogenation catalyst lifespan. Simultaneously, this method can also reduce the organic phase content in wastewater, lowering the COD and thus reducing the difficulty of wastewater treatment.

[0006] The second objective of this invention is to provide a butyraldehyde condensation reaction system that can effectively improve product purity by applying the above-mentioned separation system and combining it with enhanced mass transfer technology.

[0007] In order to achieve the above-mentioned objectives of this utility model, the following technical solution is adopted: This utility model provides a separation system for n-butyraldehyde condensation reaction liquid, including: a condensation reaction liquid pipeline, a heat exchanger, a condenser, an octenal pipeline, and an oil-water separator; the condensation reaction liquid pipeline exchanges heat with the octenal pipeline through the heat exchanger, and after being condensed by the condenser, it enters the oil-water separator through the separation inlet of the oil-water separator. The oil-water separator has a separation inlet on one side and a product outlet on the other side, and the product outlet is connected to the inlet of the octenal pipeline. The oil-water separator is equipped with an internal coalescing mesh and a baffle, which are sequentially arranged between the separation inlet and the product outlet. The baffle is vertically arranged and has a gap between its top and the top of the oil-water separator. The bottom of the oil-water separator is equipped with a separation zone water tank and an oil collection zone water tank. The separation zone water tank is located between the internal coalescing mesh and the baffle, and the oil collection zone water tank is located between the baffle and the product outlet. The bottoms of both the separation zone water tank and the oil collection zone water tank are connected to wastewater pipelines.

[0008] The above-described scheme, by incorporating an internal coalescing mesh within the oil-water separator, demulsifies the condensation reaction liquid, coalescing tiny, free water droplets into larger beads. These beads, under their own weight and the impact of the main medium, detach and settle, achieving most of the water-oil separation. By adding baffles, the oil-water separator can be divided into an oil-water separation zone and an oil collection zone. The oil phase in the upper layer of the oil-water separation zone can overflow into the oil collection zone through the baffles, achieving efficient oil phase collection. In summary, this system can achieve efficient separation of the aqueous and oil phases in the n-butyraldehyde condensation product, improving the purity and yield of octenal and reducing the water entrainment in octenal. This helps reduce the energy consumption of subsequent octenal hydrogenation and minimizes the impact on the hydrogenation catalyst lifespan. Simultaneously, this method also reduces the organic phase content in the wastewater, lowering the COD and thus reducing the difficulty of wastewater treatment.

[0009] For example, the oil-water separator is further provided with multiple layers of baffles; the multiple layers of baffles are arranged alternately along the material flow direction in the oil-water separator, and the multiple layers of baffles are disposed between the coalescing wire mesh of the inner component and the water tank of the separation zone.

[0010] This scheme, by setting up multiple layers of baffles, can extend the flow path of the condensation reaction products, slow down the flow rate of the condensation reaction products, and promote the rapid separation of the aqueous phase and oil phase in the condensation reaction products.

[0011] For example, it also includes a circulating alkali solution pipeline, the inlet of which is connected to the bottom of the oil-water separator, and the inlet of the circulating alkali solution pipeline is located between the internal coalescing mesh and the water tank of the separation zone; the separated liquid separated at the bottom of the oil-water separator flows back to the condensation reaction zone via the circulating alkali solution pipeline.

[0012] This solution, by setting up a circulating alkali solution pipeline, can improve the utilization rate of alkali solution and reduce production costs.

[0013] For example, it also includes an exhaust gas pipeline and a pressurized nitrogen pipeline; the inlet of the exhaust gas pipeline is connected to the exhaust gas outlet at the top of the oil-water separator, and the outlet of the pressurized nitrogen pipeline is connected to the nitrogen inlet at the top of the oil-water separator.

[0014] In this design, the exhaust gas pipeline and the pressurized nitrogen pipeline can form a pressure regulating assembly. In actual use, the operating pressure within the oil-water separator can be adjusted as needed (e.g., maintaining the operating pressure within the range of 0.2-1 MPa). When the actual pressure is high, exhaust gas can be released from the exhaust gas pipeline; when the actual pressure is low, nitrogen can be supplied to the oil-water separator via the pressurized nitrogen pipeline. This maintains stable pressure during the oil-water separation process, ensuring good oil-water separation efficiency.

[0015] For example, the diameter of the condensation reaction liquid pipeline gradually increases along the direction close to the oil-water separator.

[0016] This scheme gradually increases the pipe diameter, which can gradually reduce the flow rate of the condensation reaction liquid. This can prevent the liquid from impacting the stratified condensation reaction liquid in the oil-water separator, and also improve the oil-water separation efficiency of the condensation reaction liquid in the pipeline by slowing down the flow rate.

[0017] This utility model also provides a butyraldehyde condensation reaction system, including: a raw material alkali solution pipeline, a butyraldehyde pipeline, a condensation reactor, and the above-mentioned butyraldehyde condensation reaction liquid separation system; the material outlet of the condensation reactor is connected to the inlet of the condensation reaction liquid pipeline; both the raw material alkali solution pipeline and the butyraldehyde pipeline are connected to the side wall of the condensation reactor.

[0018] This scheme, by applying the above-mentioned butyraldehyde condensation reaction liquid separation system, can obtain octenal with high purity and low water content, which helps to reduce the energy consumption of subsequent octenal hydrogenation and can reduce the impact on the hydrogenation catalyst life.

[0019] For example, the condensation reactor is equipped with an enhanced reaction unit, and the raw material alkali solution pipeline passes through the side wall of the condensation reactor and is connected to the enhanced reaction unit.

[0020] This method, by setting up an enhanced reaction unit, can disperse and break the alkali solution into micron-sized microbubbles, improving the uniformity of alkali distribution in n-butyraldehyde and increasing the mass transfer area at the phase interface. This helps to improve the raw material conversion rate and product yield.

[0021] 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 raw material alkali solution pipeline 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 pipeline is located between the first enhanced mass transfer reactor and the second enhanced mass transfer reactor.

[0022] 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.

[0023] 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 pipeline.

[0024] 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.

[0025] For example, a distributor is provided inside the condensation reactor, and the outlet of the n-butyraldehyde pipeline is connected to the distributor, with the distributor outlet facing the region between the first enhanced mass transfer reactor and the second enhanced mass transfer reactor. The distributor may have orifices with different orientations.

[0026] 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.

[0027] 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.

[0028] 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.

[0029] 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.

[0030] 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.

[0031] Compared with the prior art, the beneficial effects of this utility model are as follows: 1. The above solution, by setting up an internal coalescing wire mesh in the oil-water separator, can demulsify the condensation reaction liquid, coalesce the tiny, free water droplets in the material into larger droplets, which gradually form water beads. These droplets then fall off and settle due to their own gravity and the impact force of the main medium, thus achieving most of the water-oil separation. 2. By setting up baffles, the oil-water separator can be divided into an oil-water separation zone and an oil collection zone. The oil phase in the upper layer of the oil-water separation zone can overflow into the oil collection zone through the baffle, achieving efficient collection of the oil phase. 3. In summary, the system of this scheme can achieve efficient separation of the aqueous phase and oil phase in the n-butyraldehyde condensation product, improve the purity and yield of octenal, thereby reducing the water entrained in octenal, which helps to reduce the energy consumption of subsequent octenal hydrogenation and can reduce the impact on the life of hydrogenation catalyst. 4. At the same time, this method can also reduce the content of organic phase in wastewater and lower the COD of wastewater, which helps to reduce the difficulty of wastewater treatment. Attached Figure Description

[0032] 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 This diagram shows a separation system for the n-butyraldehyde condensation reaction liquid according to Embodiment 1 of this utility model; Figure 2 A schematic diagram of the butyraldehyde condensation reaction system of Embodiment 1 of this utility model is shown.

[0033] In the diagram: 1. Raw material alkali solution pipeline; 2. Condensation reactor; 3. Second enhanced mass transfer reactor; 4. Enhanced dispersion pipe; 5. First enhanced mass transfer reactor; 6. Nitrogen sealing nitrogen pipeline; 7. Condensation reaction liquid pipeline; 8. Octenal pipeline; 9. Butyraldehyde pipeline; 10. Distributor; 11. Heat exchanger; 12. Condenser; 13. Cold water pipeline; 14. Oil-water separator; 15. Internal coalescing mesh; 16. Tail gas pipeline; 17. Pressurized nitrogen pipeline; 18. Baffle; 19. Deflector; 20. Circulating alkali solution pipeline; 21. Water tank in separation zone; 22. Wastewater pipeline; 23. Water tank in oil collection zone. Detailed Implementation

[0034] 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.

[0035] 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.

[0036] 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.

[0037] To more clearly illustrate the technical solution of this utility model, the following description is provided in the form of specific embodiments.

[0038] Example 1 See Figure 1 This embodiment provides a butyraldehyde condensation reaction liquid separation system, including: a condensation reaction liquid pipeline 7, a heat exchanger 11, a condenser 12, an octenal pipeline 8, and an oil-water separator 14; the condensation reaction liquid pipeline 7 exchanges heat with the octenal pipeline 8 via the heat exchanger 11, and after being condensed by the condenser 12, it enters the oil-water separator 14 through the separation inlet; the oil-water separator 14 has a separation inlet on one side and a product outlet on the other side, the product outlet being connected to the inlet of the octenal pipeline 8; the oil-water separator 14 is equipped with... The internal components, coalescing wire mesh 15 and baffle 19, are sequentially arranged between the separation inlet and the product outlet. The baffle 19 is vertically arranged and has a gap between the top of the oil-water separator 14. The bottom of the oil-water separator 14 is provided with a separation zone water tank 21 and an oil collection zone water tank 23. The separation zone water tank 21 is located between the internal components, coalescing wire mesh 15 and baffle 19, and the oil collection zone water tank 23 is located between the baffle 19 and the product outlet. The bottoms of both the separation zone water tank 21 and the oil collection zone water tank 23 are connected to wastewater pipes 22. In this embodiment, baffle 19 divides the oil-water separator 14 into an oil-water separation zone and an oil collection zone. The liquid level in the oil-water separator 14 continuously rises, and the top oil phase overflows into the oil collection zone through the top of baffle 19. The liquid at the bottom of the separation zone enters the water tank 21 of the separation zone for further separation, separating out the free organic phase (octenal). The wastewater at the bottom of the water tank 21 of the separation zone enters the wastewater pipeline 22. The product outlet is located in the middle of the oil collection zone. The liquid entering the oil collection zone continues to be separated in the water tank 23 of the oil collection zone. The wastewater separated at the bottom enters the wastewater pipeline 22, and the top oil phase enters the octenal pipeline 8 through the product outlet.

[0039] In this embodiment, the condensation reaction liquid generated by the butyraldehyde condensation reaction first exchanges heat with octenaldehyde in the octenaldehyde pipeline 8 to cool down to 80~100°C, and then is further cooled to 40~60°C by the condenser 12 (which is connected to the cold water pipeline 13) before entering the oil-water separator 14 for oil-water separation.

[0040] Continue reading Figure 1 The oil-water separator 14 is also provided with multiple layers of baffles 18. The multiple layers of baffles 18 are arranged alternately along the material flow direction in the oil-water separator 14, and the multiple layers of baffles 18 are arranged between the inner coalescing wire mesh 15 and the water tank 21 in the separation zone.

[0041] In this embodiment, the system further includes a circulating alkali solution pipeline 20. The inlet of the circulating alkali solution pipeline 20 is connected to the bottom of the oil-water separator 14, and the inlet of the circulating alkali solution pipeline 20 is located between the internal coalescing mesh 15 and the water tank 21 of the separation zone. The separated liquid at the bottom of the oil-water separator 14 is returned to the condensation reaction zone via the circulating alkali solution pipeline 20. In this embodiment, most of the lower aqueous phase of the oil-water separation zone is circulated back to the n-butyraldehyde condensation reaction zone (e.g., the condensation reactor 2 mentioned below), and the remaining aqueous phase is further separated by sedimentation in the water tank 21 of the separation zone to reduce the organic matter content in the separated aqueous phase.

[0042] Continue reading Figure 1 The system also includes an exhaust gas line 16 and a pressurized nitrogen line 17. The inlet of the exhaust gas line 16 is connected to the exhaust gas outlet at the top of the oil-water separator 14, and the outlet of the pressurized nitrogen line 17 is connected to the nitrogen inlet at the top of the oil-water separator 14. A pressure gauge can be installed inside the oil-water separator 14 to monitor the pressure. In actual use, the operating pressure inside the oil-water separator 14 can be adjusted as needed to maintain it within the range of 0.2-1 MPa. When the actual pressure is high, exhaust gas can be discharged through the exhaust gas line 16; when the actual pressure is low, nitrogen can be supplied to the oil-water separator 14 through the pressurized nitrogen line 17. This maintains stable pressure during the oil-water separation process, ensuring good oil-water separation efficiency.

[0043] To further improve separation efficiency, in this embodiment, the diameter of the condensation reaction liquid pipeline 7 gradually increases along the direction close to the oil-water separator 14.

[0044] This embodiment also provides a butyraldehyde condensation reaction system, such as Figure 2 As shown, the butyraldehyde condensation reaction system includes: a raw material alkali solution pipeline 1, a butyraldehyde pipeline 9, a condensation reactor 2, and the aforementioned butyraldehyde condensation reaction liquid separation system; the material outlet of the condensation reactor 2 is connected to the inlet of the condensation reaction liquid pipeline 7; both the raw material alkali solution pipeline 1 and the butyraldehyde pipeline 9 are connected to the side wall of the condensation reactor 2. A nitrogen-sealing nitrogen pipeline 6 is installed at the top of the condensation reactor 2.

[0045] Continue reading Figure 2 The condensation reactor 2 is equipped with an enhanced reaction unit, and the raw material alkali solution pipeline 1 passes through the side wall of the condensation reactor 2 and is connected to the enhanced reaction unit.

[0046] In this embodiment, the enhanced reaction unit includes a first enhanced mass transfer reactor 5 and a second enhanced mass transfer reactor 3, with the first enhanced mass transfer reactor 5 located above the second enhanced mass transfer reactor 3; the raw material alkali pipeline 1 is connected to the first enhanced mass transfer reactor 5 and the second enhanced mass transfer reactor 3 respectively; the outlets of the first enhanced mass transfer reactor 5 and the second enhanced mass transfer reactor 3 are opposite to each other, and the outlet of the n-butyraldehyde pipeline 9 is located between the first enhanced mass transfer reactor 5 and the second enhanced mass transfer reactor 3.

[0047] The outlets of the first enhanced mass transfer reactor 5 and the second enhanced mass transfer reactor 3 are connected by an enhanced dispersion pipe 4, and the enhanced dispersion pipe 4 has multiple dispersion ports on the side facing the outlet of the n-butyraldehyde pipeline 9.

[0048] Continue reading Figure 2 A distributor 10 is installed inside the condensation reactor 2. The outlet of the n-butyraldehyde pipeline 9 is connected to the distributor 10. The outlet of the distributor 10 faces the area between the first enhanced mass transfer reactor 5 and the second enhanced mass transfer reactor 3.

[0049] Tests showed that the octenal moisture content in the octenal pipeline in this embodiment was less than 0.3%wt.

[0050] 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 separation system for n-butyraldehyde condensation reaction liquid, characterized in that, include: The condensation reaction liquid pipeline includes a heat exchanger, a condenser, an octenal pipeline, and an oil-water separator. The condensation reaction liquid pipeline exchanges heat with the octenal pipeline through the heat exchanger, and after being condensed by the condenser, it enters the oil-water separator through the separation inlet. The oil-water separator has a separation inlet on one side and a product outlet on the other side, and the product outlet is connected to the inlet of the octenal pipeline. The oil-water separator is equipped with an internal coalescing mesh and a baffle, which are sequentially arranged between the separation inlet and the product outlet. The baffle is vertically arranged and has a gap between its top and the top of the oil-water separator. The bottom of the oil-water separator is equipped with a separation zone water tank and an oil collection zone water tank. The separation zone water tank is located between the internal coalescing mesh and the baffle, and the oil collection zone water tank is located between the baffle and the product outlet. The bottoms of both the separation zone water tank and the oil collection zone water tank are connected to wastewater pipelines.

2. The system according to claim 1, characterized in that, The oil-water separator is also provided with multiple layers of baffles; the multiple layers of baffles are arranged alternately along the material flow direction in the oil-water separator, and the multiple layers of baffles are arranged between the coalescing wire mesh of the inner part and the water tank of the separation zone.

3. The system according to claim 1, characterized in that, It also includes a circulating alkali solution pipeline, the inlet of which is connected to the bottom of the oil-water separator, and the inlet of the circulating alkali solution pipeline is located between the coalescing wire mesh of the inner component and the water tank of the separation zone; the separated liquid separated at the bottom of the oil-water separator flows back to the condensation reaction zone via the circulating alkali solution pipeline.

4. The system according to claim 1, characterized in that, It also includes an exhaust gas pipeline and a pressurized nitrogen pipeline; the inlet of the exhaust gas pipeline is connected to the exhaust gas outlet at the top of the oil-water separator, and the outlet of the pressurized nitrogen pipeline is connected to the nitrogen inlet at the top of the oil-water separator.

5. The system according to claim 1, characterized in that, The diameter of the condensation reaction liquid pipeline gradually increases along the direction closer to the oil-water separator.

6. A butyraldehyde condensation reaction system, characterized in that, include: The system comprises a raw material alkali solution pipeline, a n-butyraldehyde pipeline, a condensation reactor, and a n-butyraldehyde condensation reaction liquid separation system according to any one of claims 1-5; the material outlet of the condensation reactor is connected to the inlet of the condensation reaction liquid pipeline; both the raw material alkali solution pipeline and the n-butyraldehyde pipeline are connected to the side wall of the condensation reactor.

7. The system according to claim 6, characterized in that, The condensation reactor is equipped with an enhanced reaction unit, and the raw material alkali solution pipeline passes through the side wall of the condensation reactor and is connected to the enhanced reaction unit.

8. The system according to claim 7, 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 raw material alkali solution pipeline 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 pipeline is located between the first enhanced mass transfer reactor and the second enhanced mass transfer reactor.

9. The system according to claim 8, 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 tube, and the enhanced dispersion tube has multiple dispersion ports on the side facing the outlet of the n-butyraldehyde pipeline.

10. The system according to claim 8 or 9, characterized in that, A distributor is provided inside the condensation reactor, and the outlet of the n-butyraldehyde 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.

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