Device for optimizing structure of butanol and octanol product

Abstract

The utility model discloses a device for optimizing the structure of a butyl octanol product. The device is characterized in that a side line feed port of a butyraldehyde isomer tower is connected with a feed pipeline, and a tower top discharge port is respectively connected to an isobutyraldehyde hydrogenation unit and an isobutyraldehyde storage tank; a tower bottom discharge hole is connected to an n-butyraldehyde condensation unit; a gas phase extraction opening in the side wall of the tower kettle is connected to a feeding opening of an n-butyraldehyde buffer tank through a gas phase extraction pipeline, an n-butyraldehyde condenser and a first n-butyraldehyde cooler are arranged on the gas phase extraction pipeline, and a discharging opening of the n-butyraldehyde buffer tank is connected to a feeding opening of the n-butyraldehyde tank; and a discharge port of the n-butyraldehyde tank is respectively connected to the n-butyraldehyde hydrogenation unit and the n-butyraldehyde condensation unit through a first branch extraction pipeline and a second branch extraction pipeline. According to the utility model, the structure of the butanol and octanol product can be conveniently and quickly optimized, and any several of high-purity n-butyraldehyde, isobutyraldehyde, n-butyl alcohol, isobutyl alcohol and octanol can be selectively produced according to requirements.

Description

Technical Field

[0001] The utility model relates to the field of industrial production of butanol and octanol. More specifically, it relates to a device for optimizing the product structure of butanol and octanol. Background Art

[0002] In the current technology, propylene and syngas are usually used as raw materials, and a rhodium-phosphorus coordination compound is used as a catalyst for hydroformylation to produce n-butyraldehyde. Due to the recycling of the catalyst mother liquor of the rhodium-phosphorus coordination compound, the content of heavy components in the catalyst mother liquor is getting higher and higher. Inevitably, a certain amount of heavy components will be entrained in the gaseous phase crude butyraldehyde at the top of the low-pressure evaporator collection tank. Then, these heavy components will all be sent out from the bottom of the butyraldehyde isomerization column through the n-butyraldehyde pump along with the distilled n-butyraldehyde, cooled by the n-butyraldehyde cooler, and then directly sent to the condensation reactor, or sent to the n-butyraldehyde storage tank and enter the downstream process for hydrogenation or condensation-hydrogenation as an intermediate product to produce n-butanol or octanol. Since the content of heavy components in n-butyraldehyde during production is high, it is not used as a final product. Therefore, according to the demand for n-butyraldehyde products, it is necessary to produce high-purity n-butyraldehyde products.

[0003] Currently, in the industrial production of butanol and octanol, the hydroformylation mixed butyraldehyde is usually separated into n-butyraldehyde and a mixed butyraldehyde with a normal / isomer ratio of about 3.5:1. Subsequently, n-butyraldehyde is used as an intermediate for condensation-hydrogenation to produce octanol. However, due to the low purity of n-butyraldehyde produced by this process, n-butyraldehyde can only be used as an intermediate and cannot be sold as a final product. In addition to the fact that the prices of products such as n-butyraldehyde, isobutyraldehyde, n-butanol, isobutanol, and octanol fluctuate greatly due to market supply and demand relationships, this process makes it impossible to optimize the product structure according to the market orientation in actual production and selectively produce high-purity n-butyraldehyde and octanol products. Therefore, it is difficult to maximize the benefits. Summary of the Utility Model

[0004] The purpose of the utility model is to overcome the deficiencies in the prior art and propose a device for optimizing the product structure of butanol and octanol, which can conveniently and quickly optimize the product structure of butanol and octanol, and can selectively produce any several of high-purity n-butyraldehyde, isobutyraldehyde, n-butanol, isobutanol, and octanol according to requirements.

[0005] The purpose of the utility model is achieved through the following technical solutions.

[0006] The device for optimizing the product structure of butanol and octanol of the utility model comprises a butyraldehyde isomerization tower. A feed pipeline is connected to the side-line feed inlet of the butyraldehyde isomerization tower. The overhead product outlet of the butyraldehyde isomerization tower is respectively connected to an isobutyraldehyde hydrogenation unit and an isobutyraldehyde storage tank through an isobutyraldehyde product pipeline; the bottom product outlet of the butyraldehyde isomerization tower is connected to a n-butyraldehyde condensation unit through a liquid-phase n-butyraldehyde product pipeline; the gas-phase extraction outlet on the side wall of the bottom of the butyraldehyde isomerization tower is connected to the feed inlet of a n-butyraldehyde buffer tank through a gas-phase extraction pipeline. A n-butyraldehyde condenser and a first n-butyraldehyde cooler are sequentially arranged on the gas-phase extraction pipeline along the material flow direction. The discharge outlet of the n-butyraldehyde buffer tank is connected to the feed inlet of a n-butyraldehyde tank through a condensate extraction pipeline. The discharge outlet of the n-butyraldehyde tank is respectively connected to the n-butyraldehyde hydrogenation unit and the n-butyraldehyde condensation unit through a first branch extraction pipeline and a second branch extraction pipeline.

[0007] Further, a first valve is arranged on the feed pipeline.

[0008] Further, a second valve and a third valve are respectively arranged on the isobutyraldehyde product pipelines connecting the feed inlets of the isobutyraldehyde hydrogenation unit and the isobutyraldehyde storage tank.

[0009] Further, a fourteenth valve and a second n-butyraldehyde cooler are sequentially arranged on the liquid-phase n-butyraldehyde product pipeline along the liquid flow direction.

[0010] Further, a butyraldehyde isomerization tower reboiler is connected between the liquid circulation outlet and the liquid circulation inlet at the bottom of the butyraldehyde isomerization tower through a reflux pipeline.

[0011] Further, a fourth valve, a n-butyraldehyde condenser, a first n-butyraldehyde cooler and a fifth valve are sequentially arranged on the gas-phase extraction pipeline connecting the gas-phase extraction outlet and the feed inlet of the n-butyraldehyde buffer tank along the material flow direction.

[0012] Further, a sixth valve, a first n-butyraldehyde pump, an eighth valve and a tenth valve are sequentially arranged on the condensate extraction pipeline connecting the discharge outlet of the n-butyraldehyde buffer tank and the feed inlet of the n-butyraldehyde tank along the material flow direction.

[0013] Further, a spare pipeline is connected between the discharge outlet of the n-butyraldehyde buffer tank and the feed inlet of the tenth valve. A seventh valve, a second n-butyraldehyde pump and a ninth valve are sequentially arranged on the spare pipeline along the liquid flow direction.

[0014] Further, an eleventh valve is arranged at the discharge outlet of the n-butyraldehyde tank. The discharge outlet of the eleventh valve is respectively connected to the n-butyraldehyde hydrogenation unit and the n-butyraldehyde condensation unit through a first branch extraction pipeline and a second branch extraction pipeline. A twelfth valve is arranged on the first branch extraction pipeline, and a thirteenth valve is arranged on the second branch extraction pipeline.

[0015] Compared with the prior art, the beneficial effects brought by the technical solution of the present utility model are as follows:

[0016] A gas-phase extraction outlet is provided on the side wall of the bottom of the butyraldehyde isomerization tower of the present utility model, and a normal butyraldehyde side extraction line is added. After the transformation of the butyraldehyde isomerization tower is completed, high-purity normal butyraldehyde (≥99.9%) products can be side-extracted, realizing process optimization (normal butyraldehyde products could not be extracted before the transformation). High-purity n-butanol (≥99.9%) products can be produced (the purity was about 99.6% before the transformation), high-purity octanol (≥99.9%) products can be produced (the purity was about 99.6% before the transformation), high-purity n-butanol (≥99.9%) products can be produced (the purity was about 99.6% before the transformation). Also, according to market conditions, normal butyraldehyde, n-butanol, and octanol products can be selectively produced, realizing product diversification. BRIEF DESCRIPTION OF THE DRAWINGS

[0017] Figure 1 It is a schematic diagram of the device for optimizing the product structure of butanol and octanol of the present utility model.

[0018] Reference numerals: 1 - feed pipeline, 2 - first valve, 3 - side-line feed port, 4 - butyraldehyde isomerization tower, 5 - isobutyraldehyde discharge pipeline, 6 - second valve, 7 - third valve, 8 - isobutyraldehyde hydrogenation unit, 9 - isobutyraldehyde storage tank, 10 - gas-phase extraction outlet, 11 - gas-phase extraction pipeline, 12 - fourth valve, 13 - normal butyraldehyde condenser, 14 - first normal butyraldehyde cooler, 15 - fifth valve, 16 - normal butyraldehyde buffer tank, 17 - sixth valve, 18 - seventh valve, 19 - first butyraldehyde pump, 20 - second butyraldehyde pump, 21 - eighth valve, 22 - ninth valve, 23 - condensate extraction pipeline, 24 - tenth valve, 25 - normal butyraldehyde tank, 26 - eleventh valve, 27 - first branch extraction pipeline, 28 - twelfth valve, 29 - normal butyraldehyde hydrogenation unit, 30 - second branch extraction pipeline, 31 - thirteenth valve, 32 - normal butyraldehyde condensation unit, 33 - reflux pipeline (in the direction of 33 - 34), 34 - butyraldehyde isomerization tower reboiler, 35 - liquid-phase normal butyraldehyde discharge pipeline, 36 - fourteenth valve, 37 - second normal butyraldehyde cooler. DETAILED DESCRIPTION OF THE EMBODIMENTS

[0019] The present utility model will be further described below with reference to the drawings.

[0020] As Figure 1As shown in the figure, the device for optimizing the product structure of butanol and octanol of the present utility model includes a butyraldehyde isomerization tower 4. A feed pipeline 1 is connected to the side-line feed port 3 of the butyraldehyde isomerization tower 4. The top discharge port of the butyraldehyde isomerization tower 4 is respectively connected to an isobutyraldehyde hydrogenation unit 8 and an isobutyraldehyde storage tank 9 through an isobutyraldehyde discharge pipeline 5. The bottom discharge port of the butyraldehyde isomerization tower 4 is connected to a n-butyraldehyde condensation unit 32 through a liquid-phase n-butyraldehyde discharge pipeline 35. The gas-phase extraction port 10 on the side wall of the bottom of the butyraldehyde isomerization tower 4 is connected to the feed port of a n-butyraldehyde buffer tank 16 through a gas-phase extraction pipeline 11. And a n-butyraldehyde condenser 13 and a first n-butyraldehyde cooler 14 are sequentially arranged on the gas-phase extraction pipeline 11 along the material flow direction. The discharge port of the n-butyraldehyde buffer tank 16 is connected to the feed port of a n-butyraldehyde tank 25 through a condensate extraction pipeline 23. The discharge port of the n-butyraldehyde tank 25 is respectively connected to a n-butyraldehyde hydrogenation unit 29 and a n-butyraldehyde condensation unit 32 through a first branch extraction pipeline 27 and a second branch extraction pipeline 30.

[0021] In the above device, preferably, the determination process of the position of the gas-phase extraction port 10 on the side wall of the bottom of the butyraldehyde isomerization tower 4: The Aspen Plus simulation software can be used to perform a process simulation calculation on the gas-phase side extraction of n-butyraldehyde under various retrofit schemes when the feed load is 24000 kg / h. Finally, the position of the gas-phase extraction port 10 of the butyraldehyde isomerization tower 4 is determined to be 450 mm vertically downward from the last tray counted from top to bottom.

[0022] In the above device, preferably, a first valve 2 can be arranged on the feed pipeline 1.

[0023] In the above device, preferably, a second valve 6 and a third valve 7 can be respectively arranged on the isobutyraldehyde discharge pipeline 5 connected to the feed ports of the isobutyraldehyde hydrogenation unit 8 and the isobutyraldehyde storage tank 9.

[0024] In the above device, preferably, a fourteenth valve 36 and a second n-butyraldehyde cooler 37 can be sequentially arranged on the liquid-phase n-butyraldehyde discharge pipeline 35 along the liquid flow direction.

[0025] In the above device, preferably, a butyraldehyde isomerization tower reboiler 34 can be connected between the liquid circulation outlet and the liquid circulation inlet at the bottom of the butyraldehyde isomerization tower 4 through a reflux pipeline 33.

[0026] In the above device, preferably, a fourth valve 12, a n-butyraldehyde condenser 13, a first n-butyraldehyde cooler 14, and a fifth valve 15 can be sequentially arranged on the gas-phase extraction pipeline 11 connected between the gas-phase extraction port 10 and the feed port of the n-butyraldehyde buffer tank 16 along the material flow direction.

[0027] In the above device, preferably, a sixth valve 17, a first butyraldehyde pump 19, an eighth valve 21, and a tenth valve 24 may be sequentially arranged on the condensate extraction pipeline 23 connected between the outlet of the n-butyraldehyde buffer tank 16 and the inlet of the n-butyraldehyde tank 25 along the material flow direction. A spare pipeline may be connected between the outlet of the n-butyraldehyde buffer tank 16 and the inlet of the tenth valve 24, and a seventh valve 18, a second butyraldehyde pump 20, and a ninth valve 22 may be sequentially arranged on the spare pipeline along the liquid flow direction.

[0028] In the above device, preferably, an eleventh valve 26 may be arranged at the outlet of the n-butyraldehyde tank 25. The outlet of the eleventh valve 26 may be connected to the n-butyraldehyde hydrogenation unit 29 and the n-butyraldehyde condensation unit 32 through a first branch extraction pipeline 27 and a second branch extraction pipeline 30 respectively. A twelfth valve 28 may be arranged on the first branch extraction pipeline 27, and a thirteenth valve 31 may be arranged on the second branch extraction pipeline 30.

[0029] In the above device, preferably, the top operating pressure of the butyraldehyde isomerization tower 4 may be 141 - 165 kPa, the top temperature may be 74.3 - 79.3 °C, and the bottom temperature may be 94.4 - 98.8 °C.

[0030] The optimized production process of the above device for optimizing the structure of butanol and octanol products of the present utility model is as follows:

[0031] ① When a high-purity n-butyraldehyde product is required, the first valve 2, the second valve 6, the third valve 7, the fourth valve 12, the fifth valve 15, the tenth valve 24, and the fourteenth valve 36 are in the "open" state, and the sixth valve 17 and the eighth valve 21 are simultaneously in the "open" state (or the seventh valve 18 and the ninth valve 22 are simultaneously in the "open" state); the eleventh valve 26, the twelfth valve 28, and the thirteenth valve 31 are in the "closed" state, and the seventh valve 18 and the ninth valve 22 are simultaneously in the "closed" state (or the sixth valve 17 and the eighth valve 21 are simultaneously in the "closed" state).

[0032] A mixed butyraldehyde raw material with a normal / iso ratio of 7:1 to 10:1 enters the butyraldehyde isomerization tower 4 through a feed pipeline 1 equipped with a first valve 2 and a side feed port 3 at the 50th to 64th trays from top to bottom. After rectification separation, high-purity isobutyraldehyde is obtained at the top of the tower and sent to the isobutyraldehyde hydrogenation unit 8 through an isobutyraldehyde discharge pipeline 5 to produce isobutanol or directly sent to an isobutyraldehyde storage tank 9; a part of the normal butyraldehyde gas-phase material is taken out from a gas-phase extraction port 10 on the side wall of the bottom of the tower, enters a normal butyraldehyde condenser 13 through a gas-phase extraction pipeline 11 for condensation, and after the condensate is cooled to 45 °C or below 45 °C by a first normal butyraldehyde cooler 14, the obtained high-purity normal butyraldehyde condensate stabilizes the flow rate of normal butyraldehyde through a normal butyraldehyde buffer tank 16, and then the high-purity normal butyraldehyde condensate is taken out through a condensate extraction pipeline 23 by a first butyraldehyde pump 19 (or a second butyraldehyde pump 20) and sent to a normal butyraldehyde tank 25; a part of the normal butyraldehyde liquid-phase material and heavy components at the bottom of the tower return to the butyraldehyde isomerization tower 4 through a reflux pipeline 33 and a butyraldehyde isomerization tower reboiler 34 as reflux, and a part is transported to a subsequent normal butyraldehyde condensation unit 32 through a liquid-phase normal butyraldehyde discharge pipeline 35 and a normal butyraldehyde cooler 37 for the production of octanol products. Through the above optimization process, the molar percentage purities of the product normal butyraldehyde, the product isobutyraldehyde, and the product isobutanol are all not less than 99.9%.

[0033] ② When high-purity n-butanol products are required, the first valve 2, the second valve 6, the third valve 7, the fourth valve 12, the fifth valve 15, the tenth valve 24, the eleventh valve 26, the twelfth valve 28, and the fourteenth valve 36 are in the "open" state, and the sixth valve 17 and the eighth valve 21 are simultaneously in the "open" state (or the seventh valve 18 and the ninth valve 22 are simultaneously in the "open" state); the thirteenth valve 31 is in the "closed" state, and the seventh valve 18 and the ninth valve 22 are simultaneously in the "closed" state (or the sixth valve 17 and the eighth valve 21 are simultaneously in the "closed" state).

[0034] The mixed butyraldehyde raw material with a normal / iso ratio of 7:1 to 10:1 enters the butyraldehyde isomerization tower 4 through the feed pipeline 1 equipped with the first valve 2 and the side feed port 3 at the 50th to 64th trays from top to bottom. After rectification separation, high-purity isobutyraldehyde is obtained at the top of the tower and sent to the isobutyraldehyde hydrogenation unit 8 through the isobutyraldehyde discharge pipeline 5 to produce isobutanol or directly sent to the isobutyraldehyde storage tank 9; a part of the normal butyraldehyde gas-phase material is taken out from the gas-phase extraction port 10 on the side wall of the tower bottom, enters the normal butyraldehyde condenser 13 through the gas-phase extraction pipeline 11 for condensation, and after the condensate is cooled to 45 °C or below 45 °C by the first normal butyraldehyde cooler 14, the obtained high-purity normal butyraldehyde condensate stabilizes the flow rate of normal butyraldehyde through the normal butyraldehyde buffer tank 16. Then, the high-purity normal butyraldehyde condensate is taken out through the condensate extraction pipeline 23 by the first butyraldehyde pump 19 (or the second butyraldehyde pump 20) and sent to the normal butyraldehyde tank 25. The high-purity normal butyraldehyde product in the normal butyraldehyde tank 25 is taken out through the first branch extraction pipeline 27 and sent to the subsequent normal butyraldehyde hydrogenation unit 29 to produce a high-purity n-butanol product; a part of the normal butyraldehyde liquid-phase material and heavy components at the tower bottom return to the butyraldehyde isomerization tower 4 through the reflux pipeline 33 and the butyraldehyde isomerization tower reboiler 34 as reflux, and a part enters the subsequent normal butyraldehyde condensation unit 32 through the liquid-phase normal butyraldehyde discharge pipeline 35 and the second normal butyraldehyde cooler 37 for producing octanol products. Through the above optimization process, the molar percentage purities of the product normal butyraldehyde, product isobutyraldehyde, product isobutanol, and product n-butanol are all not less than 99.9%.

[0035] ③ When high-purity octanol products are required, the first valve 2, the second valve 6, the third valve 7, the fourth valve 12, the fifth valve 15, the tenth valve 24, the eleventh valve 26, and the thirteenth valve 31 are in the "open" state, and the sixth valve 17 and the eighth valve 21 are simultaneously in the "open" state (or the seventh valve 18 and the ninth valve 22 are simultaneously in the "open" state); the twelfth valve 28 and the fourteenth valve 36 are in the "closed" state, and the seventh valve 18 and the ninth valve 22 are simultaneously in the "closed" state (or the sixth valve 17 and the eighth valve 21 are simultaneously in the "closed" state).

[0036] The mixed butyraldehyde raw material with a normal / iso ratio of 7:1 to 10:1 enters the butyraldehyde isomerization column 4 through the feed pipeline 1 equipped with the first valve 2 and the side feed port 3 at the 50th to 64th trays counted from top to bottom. After rectification and separation, high-purity isobutyraldehyde is obtained at the top of the column and sent to the isobutyraldehyde hydrogenation unit 8 through the isobutyraldehyde discharge pipeline 5 to produce isobutanol or directly sent to the isobutyraldehyde storage tank 9; the normal butyraldehyde gas-phase material is side-drawn from the gas-phase extraction port 10 on the side wall of the bottom of the column, enters the normal butyraldehyde condenser 13 through the gas-phase extraction pipeline 11 for condensation, and after the condensate is cooled to 45°C or below 45°C by the first normal butyraldehyde cooler 14, the high-purity normal butyraldehyde condensate stabilizes the flow rate of normal butyraldehyde through the normal butyraldehyde buffer tank 16. Then, the high-purity normal butyraldehyde condensate is drawn out through the condensate extraction pipeline 23 by the first butyraldehyde pump 19 (or the second butyraldehyde pump 20) to the normal butyraldehyde tank 25. The high-purity normal butyraldehyde product in the normal butyraldehyde tank 25 is drawn out through the second branch extraction pipeline 30 to the subsequent normal butyraldehyde condensation unit 32 for producing high-purity octanol products; the normal butyraldehyde liquid-phase material and heavy components at the bottom of the column return to the butyraldehyde isomerization column 4 through the reflux pipeline 33 and the butyraldehyde isomerization column reboiler 34 as reflux. Through the above optimization process, the molar percentage purities of the product normal butyraldehyde, product isobutyraldehyde, product isobutanol, and product octanol are all not less than 99.9%.

[0037] ④ When high-purity n-butanol and octanol products are required, the first valve 2, the second valve 6, the third valve 7, the fourth valve 12, the fifth valve 15, the tenth valve 24, the eleventh valve 26, the twelfth valve 28, and the thirteenth valve 31 are in the "open" state, and the sixth valve 17 and the eighth valve 21 are both in the "open" state (or the seventh valve 18 and the ninth valve 22 are both in the "open" state); the fourteenth valve 36 is in the "closed" state, and the seventh valve 18 and the ninth valve 22 are both in the "closed" state (or the sixth valve 17 and the eighth valve 21 are both in the "closed" state).

[0038] A mixed butyraldehyde raw material with a normal / iso ratio of 7:1 to 10:1 enters the butyraldehyde isomerization column 4 through a feed pipeline 1 equipped with a first valve 2 and a side feed port 3 at the 50th to 64th trays counted from the top downwards. After rectification separation, high-purity isobutyraldehyde is obtained at the top of the column and sent to the isobutyraldehyde hydrogenation unit 8 through an isobutyraldehyde discharge pipeline 5 to produce isobutanol or directly sent to an isobutyraldehyde storage tank 9; a normal butyraldehyde gas-phase material is side-drawn from the gas-phase extraction port 10 on the side wall of the bottom of the column, enters a normal butyraldehyde condenser 13 through a gas-phase extraction pipeline 11 for condensation. After the condensate is cooled to 45°C or below 45°C by a first normal butyraldehyde cooler 14, the obtained high-purity normal butyraldehyde condensate stabilizes the flow rate of normal butyraldehyde through a normal butyraldehyde buffer tank 16. Then, the high-purity normal butyraldehyde condensate is extracted through a condensate extraction pipeline 23 by a first butyraldehyde pump 19 (or a second butyraldehyde pump 20) to a normal butyraldehyde tank 25. The normal butyraldehyde product in the normal butyraldehyde tank 25 enters a subsequent normal butyraldehyde hydrogenation unit 29 and a normal butyraldehyde condensation unit 32 through a first branch extraction pipeline 27 and a second branch extraction pipeline 30 respectively, and is used to produce high-purity normal butanol and octanol products; the normal butyraldehyde liquid-phase material and heavy components at the bottom of the column return to the butyraldehyde isomerization column 4 through a reflux pipeline 33 and a butyraldehyde isomerization column reboiler 34 as reflux. Through the above optimization process, the molar percentage purities of the product normal butyraldehyde, product isobutyraldehyde, product normal butanol, product isobutanol, and product octanol are all not less than 99.9%.

[0039] Although the functions and working processes of the present utility model have been described above in conjunction with the accompanying drawings, the present utility model is not limited to the above specific functions and working processes. The above specific embodiments are merely illustrative and not restrictive. Under the inspiration of the present utility model, those of ordinary skill in the art can also make many forms without departing from the purpose of the present utility model and the scope protected by the claims. All of these fall within the protection scope of the present utility model.

Claims

1. An apparatus for optimizing the product structure of butanol and octanol, comprising a butyraldehyde isomer tower (4), wherein a side line feed port (3) of the butyraldehyde isomer tower (4) is connected to a feed pipeline (1), and is characterized in that, The top discharge port of the butyraldehyde isomerization column (4) is connected to the isobutyraldehyde hydrogenation unit (8) and the isobutyraldehyde storage tank (9) respectively through an isobutyraldehyde discharge pipeline (5); the bottom discharge port of the butyraldehyde isomerization column (4) is connected to the n-butyraldehyde condensation unit (32) through a liquid-phase n-butyraldehyde discharge pipeline (35); the gas-phase extraction port (10) on the side wall of the column kettle of the butyraldehyde isomerization column (4) is connected to the feed port of the n-butyraldehyde buffer tank (16) through a gas-phase extraction pipeline (11), and a n-butyraldehyde condenser (13) and a first n-butyraldehyde cooler (14) are arranged in sequence along the material flow direction on the gas-phase extraction pipeline (11). The discharge port of the n-butyraldehyde buffer tank (16) is connected to the feed port of the n-butyraldehyde tank (25) through a condensate extraction pipeline (23). The discharge port of the n-butyraldehyde tank (25) is connected to the n-butyraldehyde hydrogenation unit (29) and the n-butyraldehyde condensation unit (32) respectively through a first branch extraction pipeline (27) and a second branch extraction pipeline (30).

2. The device for optimizing the product structure of butanol and octanol according to claim 1, characterized in that, A first valve (2) is arranged on the feed pipeline (1).

3. The device for optimizing the product structure of butanol and octanol according to claim 1, wherein A second valve (6) and a third valve (7) are respectively arranged on the isobutyraldehyde discharge pipeline (5) connected to the feed ports of the isobutyraldehyde hydrogenation unit (8) and the isobutyraldehyde storage tank (9).

4. The device for optimizing the product structure of butanol and octanol according to claim 1, characterized in that, A fourteenth valve (36) and a second n-butyraldehyde cooler (37) are arranged in sequence along the liquid flow direction on the liquid-phase n-butyraldehyde discharge pipeline (35).

5. The device for optimizing the product structure of butanol and octanol according to claim 1, characterized in that, A butyraldehyde isomerization column reboiler (34) is connected between the liquid circulation outlet and the liquid circulation inlet at the bottom of the butyraldehyde isomerization column (4) through a reflux pipeline (33).

6. The device for optimizing the product structure of butanol and octanol according to claim 1, characterized in that, A fourth valve (12), a n-butyraldehyde condenser (13), a first n-butyraldehyde cooler (14), and a fifth valve (15) are arranged in sequence along the material flow direction on the gas-phase extraction pipeline (11) connecting the gas-phase extraction port (10) and the feed port of the n-butyraldehyde buffer tank (16).

7. The device for optimizing the product structure of butanol and octanol according to claim 1, characterized in that, A sixth valve (17), a first butyraldehyde pump (19), an eighth valve (21), and a tenth valve (24) are arranged in sequence along the material flow direction on the condensate extraction pipeline (23) connecting the discharge port of the n-butyraldehyde buffer tank (16) and the feed port of the n-butyraldehyde tank (25).

8. The device for optimizing the product structure of butanol and octanol according to claim 7, characterized in that, A spare pipeline is connected between the discharge port of the n-butyraldehyde buffer tank (16) and the feed port of the tenth valve (24), and a seventh valve (18), a second butyraldehyde pump (20), and a ninth valve (22) are arranged in sequence along the liquid flow direction on the spare pipeline.

9. The device for optimizing the product structure of butanol and octanol according to claim 1, characterized in that, An eleventh valve (26) is arranged at the discharge port of the n-butyraldehyde tank (25). The discharge port of the eleventh valve (26) is connected to the n-butyraldehyde hydrogenation unit (29) and the n-butyraldehyde condensation unit (32) respectively through a first branch extraction pipeline (27) and a second branch extraction pipeline (30). A twelfth valve (28) is arranged on the first branch extraction pipeline (27), and a thirteenth valve (31) is arranged on the second branch extraction pipeline (30).

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