Methanol steam recycling device for producing sodium methoxide

Abstract

The utility model relates to a methanol steam recycling device for producing sodium methoxide, which comprises a sodium methoxide synthesis tower, a first methanol steam delivery pipe and a tail gas delivery pipe are arranged on the sodium methoxide synthesis tower, a compressor, a superheater and a first regulating valve are arranged on the first methanol steam delivery pipe, and a rectifying tower is arranged on the tail gas delivery pipe. The rectifying tower is provided with a tower top condenser, the tower top condenser is communicated with an adsorption tank and a liquid methanol conveying header pipe, a molecular sieve layer is arranged in the adsorption tank, the adsorption tank is provided with a second methanol steam conveying pipe, and the liquid methanol conveying header pipe is provided with a liquid methanol conveying branch pipe; a first stop valve and a methanol vaporizer are arranged on the liquid methanol conveying branch pipe; and buffer tanks are arranged on the methanol vaporizer, the second methanol steam conveying pipe, the tower top condenser heat source channel and the first methanol steam conveying pipe. And the water content of methanol steam conveyed to the sodium methoxide synthesis tower is reduced. The utility model has the advantages of convenient use and wide market prospect.

Description

Technical Field

[0001] This utility model relates to the field of methanol vapor recovery and utilization equipment, specifically to a methanol vapor recovery and utilization device for producing sodium methoxide. Background Technology

[0002] Sodium methoxide is the most basic sodium alkoxide, also known as sodium methoxy. It is a white powder at room temperature and pressure, while sodium methoxide solution is a colorless, viscous liquid with a boiling point greater than 450℃ and a relative density of 1.31 g / cm³. It is soluble in methanol and ethanol and readily soluble in water. Currently, there are two main production methods: the metallic sodium method and the alkaline method. The metallic sodium method involves the direct reaction of solid or molten metallic sodium with lower alcohols to produce sodium methoxide and hydrogen gas. The advantages of this method are high purity of the sodium methoxide product, simple process, and low equipment cost. The disadvantages are safety concerns, as the generated hydrogen gas is highly explosive, and the raw material, metallic sodium, is very reactive and expensive. The alkaline method involves the reaction of methanol and sodium hydroxide to produce sodium methoxide and water. The advantages of this method are cheap and readily available raw materials, lower cost, and safer operation. However, because it is a reversible reaction, it is prone to incomplete reaction, and the product often contains impurities such as sodium hydroxide. Therefore, alkaline production requires continuous removal of water and the addition of catalysts to drive the reaction as much as possible towards the product, while also performing separation operations such as distillation to minimize impurities.

[0003] The tail gas emitted from the top of the sodium methoxide synthesis tower contains a large amount of methanol and a small amount of water. In the alkaline process for synthesizing sodium methoxide, this tail gas must be collected, dehydrated, and reused; otherwise, a large amount of raw material will be wasted, leading to excessively high costs for the produced sodium methoxide. In the alkaline process for synthesizing sodium methoxide, the methanol feed gas is first used as a heat source to remove water from the distilled material, thus obtaining relatively high-purity liquid sodium methoxide. In this process, the heat of liquefaction of methanol vapor is used to heat the distilled material, causing the water in the material to convert into gas and rise with the gas stream to form the tail gas at the top of the sodium methoxide synthesis tower. Specifically, the methanol vapor, due to liquefaction, descends along with the descending liquid stream of the distilled material. Therefore, the methanol vapor delivered to the sodium methoxide synthesis tower must at least meet the minimum moisture content requirements for liquid sodium methoxide to synthesize liquid sodium methoxide with the required moisture content. Of course, if you want to increase the proportion of qualified liquid sodium methoxide produced and reduce the occurrence of re-distillation due to excessive moisture, it is undoubtedly possible to increase the proportion of liquid sodium methoxide with the lowest possible moisture content by introducing methanol vapor into the sodium methoxide synthesis tower.

[0004] However, existing technology has shown that although distillation can remove moisture from methanol vapor, due to the azeotropic phenomenon between methanol and water, it is difficult to obtain methanol vapor with very low moisture content simply by relying on rectification. Therefore, there is room for improvement in the existing technology to reduce the water content of the methanol vapor fed into the sodium methoxide synthesis tower, thereby increasing the qualified rate of liquid sodium methoxide products, reducing the need for re-rectification due to excessive moisture, and thus comprehensively reducing the consumption costs of sodium methoxide production and improving the market competitiveness of sodium methoxide products. Summary of the Invention

[0005] To address the shortcomings of existing technologies, this invention provides a methanol vapor recovery and utilization device for sodium methoxide production that can reduce the water content of methanol vapor transported to the sodium methoxide synthesis tower, thereby overcoming the deficiencies in existing technologies.

[0006] The technical solution adopted by this utility model is as follows: a methanol vapor recovery and utilization device for producing sodium methoxide, comprising a sodium methoxide synthesis tower, wherein a first methanol vapor conveying pipe and a tail gas conveying pipe are provided on the sodium methoxide synthesis tower, wherein a compressor, a superheater and a first regulating valve are sequentially arranged on the first methanol vapor conveying pipe from away from the sodium methoxide synthesis tower to near the sodium methoxide synthesis tower, a distillation tower is provided on the tail gas conveying pipe, a top condenser is provided at the top of the distillation tower, the heat source channel of the top condenser is connected to the inner cavity of the distillation tower, an adsorption tank is connected at the top of the heat source channel of the top condenser, a molecular sieve layer is provided in the adsorption tank, the inlet end of a second methanol vapor conveying pipe is provided on the adsorption tank, a liquid methanol conveying main pipe is provided at the inlet end of the heat source channel of the top condenser, a liquid methanol conveying branch pipe is provided on the liquid methanol conveying main pipe, a first shut-off valve and the inlet end of a methanol vaporizer are provided on the liquid methanol conveying branch pipe, and a buffer tank is provided at the outlet end of the methanol vaporizer, the second methanol vapor conveying pipe, the outlet end of the heat source channel of the top condenser and the first methanol vapor conveying pipe.

[0007] Preferably, the liquid methanol delivery main is provided with a liquid flow sensor, a second regulating valve and a first booster pump in sequence along the direction from near the top condenser to away from the top condenser; a first gas flow sensor is provided on the tail gas delivery pipe; and a second gas flow sensor is provided on the first methanol vapor delivery pipe between the first regulating valve and the sodium methoxide synthesis tower.

[0008] Preferably, a first online chromatograph is installed on the second methanol vapor delivery pipe.

[0009] Preferably, the number of adsorption tanks is at least two, each adsorption tank is equipped with a molecular sieve layer, each adsorption tank has an outlet end of a first conveying pipe at its inlet end, the inlets of several first conveying pipes are connected to the top of the heat source channel of the tower top condenser, each adsorption tank has an inlet end of a second conveying pipe at its outlet end, the outlet ends of several second conveying pipes are connected to the inlet end of a second methanol vapor conveying pipe, and each of the several second conveying pipes and the several first conveying pipes is equipped with a second shut-off valve.

[0010] Preferably, the inner cavity of the distillation column is provided with a first packing layer, a reflux nozzle, a baffle, a second packing layer, and a third packing layer in sequence from bottom to top. The baffle is provided with a plurality of gas lifting caps. The outlet end of the distillation column and the tail gas delivery pipe between the second packing layer and the third packing layer are connected. A first circulation pipe is provided on the distillation column between the baffle and the second packing layer, as well as on the distillation column between the second packing layer and the third packing layer. A second booster pump, the inlet end of a condensate delivery pipe, a third regulating valve, and a first reboiler are provided in sequence along the direction from the inlet end of the first circulation pipe to the outlet end of the first circulation pipe. A fourth regulating valve is provided on the condensate delivery pipe. The outlet end of the condensate delivery pipe is connected to the inlet end of the reflux nozzle.

[0011] Preferably, a second circulation pipe is provided on the distillation column below the third packing layer, with the outlet end of the second circulation pipe located below the inlet end of the second circulation pipe. Along the direction from the inlet end to the outlet end of the second circulation pipe, a second online chromatograph, a third circulation pump, the inlet end of the waste liquid discharge pipe, a fifth regulating valve, and a second reboiler are sequentially arranged. A sixth regulating valve is provided on the waste liquid discharge pipe.

[0012] The beneficial effects of this utility model are as follows: First, this utility model reduces the water content in the tail gas by distillation in a distillation tower, forming a gas to be adsorbed, which is then transported to an adsorption tank in operation. Under the adsorption of the molecular sieve layer in the adsorption tank, anhydrous methanol gas is formed and sent back to the sodium methoxide synthesis tower to participate in the synthesis of sodium methoxide. This solves the technical difficulty of not being able to obtain anhydrous methanol vapor by simply using distillation, and also reduces the technical problem of excessively high frequency of molecular sieve desorption and regeneration due to the high water content in the tail gas when simply using molecular sieve adsorption. It is worthy of promotion and application.

[0013] Secondly, the second methanol vapor transmission pipe of this invention is equipped with a first online chromatograph and a third gas flow sensor; the installation of the third gas flow sensor facilitates feedback on the flow parameters of the gas medium transported through the second methanol vapor transmission pipe.

[0014] Furthermore, the liquid methanol delivery main pipe of this utility model is provided with a liquid flow sensor, a second regulating valve and a first booster pump in sequence along the direction from near the top condenser to away from the top condenser. The installation of the liquid flow sensor facilitates feedback on the flow parameters of the liquid medium delivered through the liquid methanol delivery main pipe.

[0015] This utility model has a simple structure, is easy to operate, and has a clever design, which greatly improves work efficiency and has good social and economic benefits. It is a product that is easy to promote and use. Attached Figure Description

[0016] Figure 1 This is a schematic diagram of the structure of this utility model.

[0017] Figure 2 for Figure 1 A magnified view of detail A. Detailed Implementation

[0018] like Figure 1 and Figure 2 As shown, a methanol vapor recovery and utilization device for producing sodium methoxide includes a sodium methoxide synthesis tower 1. The sodium methoxide synthesis tower 1 is equipped with a first methanol vapor delivery pipe 2 and a tail gas delivery pipe 3. A compressor 4, a superheater 5, and a first regulating valve 6 are sequentially arranged on the first methanol vapor delivery pipe 2 from the direction away from the sodium methoxide synthesis tower 1 to the direction closer to the sodium methoxide synthesis tower 1. A distillation tower 7 is installed on the tail gas delivery pipe 3. A top condenser 8 is installed at the top of the distillation tower 7. The heat source channel of the top condenser 8 is connected to the inner cavity of the distillation tower 7. The top of the heat source channel of the top condenser 8... An adsorption tank 9 is connected to the tower, and a molecular sieve layer 10 is installed inside the adsorption tank 9. The inlet end of the second methanol vapor delivery pipe 11 is installed on the adsorption tank 9. A liquid methanol delivery main pipe 12 is installed on the inlet end of the heat source channel of the tower top condenser 8. A liquid methanol delivery branch pipe 13 is installed on the liquid methanol delivery main pipe 12. A first shut-off valve 14 and the inlet end of the methanol vaporizer 15 are installed on the liquid methanol delivery branch pipe 13. A buffer tank 16 is installed on the outlet end of the methanol vaporizer 15, the second methanol vapor delivery pipe 11, the outlet end of the heat source channel of the tower top condenser 8, and the first methanol vapor delivery pipe 2. A liquid flow sensor 17, a second regulating valve 18, and a first booster pump 19 are sequentially installed on the liquid methanol delivery main pipe 12 along the direction from near the tower top condenser 8 to away from the tower top condenser 8. A first gas flow sensor 20 is installed on the tail gas delivery pipe 3. A second gas flow sensor 21 is installed on the first methanol vapor delivery pipe 2 between the first regulating valve 6 and the sodium methoxide synthesis tower 1.

[0019] The number of adsorption tanks 9 is at least two. Each adsorption tank 9 is equipped with a molecular sieve layer 10. The inlet end of each adsorption tank 9 is provided with the outlet end of a first conveying pipe 23. The inlet ends of several first conveying pipes 23 are connected to the top of the heat source channel of the tower top condenser 8. The outlet end of each adsorption tank 9 is provided with the inlet end of a second conveying pipe 24. The outlet ends of several second conveying pipes 24 are connected to the inlet end of a second methanol vapor conveying pipe 11. A second shut-off valve 25 is provided on several second conveying pipes 24 and several first conveying pipes 23.

[0020] The second methanol vapor delivery pipe 11 is equipped with a first online chromatograph 22 and a third gas flow sensor 45; the installation of the first online chromatograph 22 facilitates the feedback of component parameters. This, in turn, informs the operator whether the molecular sieve layer 10 in the currently used adsorption tank 9 can properly adsorb the small amount of moisture in the methanol vapor.

[0021] In existing technologies, at least two distillation columns are typically required to fully distill the liquefied medium from the tail gas discharged from the tail gas conveying pipe 3 of the sodium methoxide synthesis column 1. Otherwise, the methanol content in the discharged wastewater will be too high, resulting in waste of raw materials. However, two distillation columns occupy a relatively large area, and there are relatively many pipes connecting the two distillation columns, making the structure more complex. To address the above issues, the distillation column 7 of this product is provided with a first packing layer 26, a reflux nozzle 27, a baffle 28, a second packing layer 29, and a third packing layer 30 arranged sequentially from bottom to top in the inner cavity. Several gas risers are provided on the baffle 28. The outlet end of the distillation column 7 between the second packing layer 29 and the third packing layer 30 is connected to the cap 31. The distillation column 7 between the partition plate 28 and the second packing layer 29, as well as the distillation column 7 between the second packing layer 29 and the third packing layer 30, are provided with a first circulation pipe 32. The first circulation pipe 32 is provided with a second booster pump 33, the inlet end of the condensate delivery pipe 34, a third regulating valve 35, and a first reboiler 36 in sequence along the direction from the inlet end of the first circulation pipe 32 to the outlet end of the first circulation pipe 32. The condensate delivery pipe 34 is provided with a fourth regulating valve 37. The outlet end of the condensate delivery pipe 34 is connected to the inlet end of the reflux nozzle 27. Furthermore, a second circulation pipe 38 is provided on the distillation column 7 below the third packing layer 30. The outlet end of the second circulation pipe 38 is located below the inlet end of the second circulation pipe 38. Along the direction from the inlet end to the outlet end of the second circulation pipe 38, a second online chromatograph 39, a third circulation pump 40, the inlet end of the waste liquid discharge pipe 41, a fifth regulating valve 42, and a second reboiler 43 are arranged in sequence. A sixth regulating valve 44 is provided on the waste liquid discharge pipe 41.

[0022] Using the baffle 28 and several lifting caps 31 as partitions, the rising gas flow below the baffle 28 is transported through the lifting caps 31 to the second packing layer 29 for re-distillation. The descending liquid flow from the second packing layer 29 is blocked by the baffle 28 and the lifting caps 31 and is transported through the first circulation pipe 32. Part of it is used as reflux condensate of the rising gas flow below the baffle 28, and the other part is reheated to form a gas-liquid mixture, which is then transported to the distillation column 7 between the second packing layer 29 and the third packing layer 30 for distillation. This creates several methanol concentration zones in the distillation column 7, so that the methanol concentration in the distillation column 7 gradually increases with the height of the distillation column 7. As a result, a liquid enrichment zone with low methanol content is formed at the bottom of the distillation column 7. When the methanol content in this liquid enrichment zone is lower than the preset standard, it can be discharged.

[0023] The usage instructions for this product are as follows: Figure 1 and Figure 2 As shown, the specific steps include:

[0024] S1. During the start-up phase of the sodium methoxide synthesis tower 1, anhydrous methanol is delivered to the liquid methanol delivery main pipe 12 and divided into two parts: a first part of anhydrous methanol and a second part of anhydrous methanol. The first part of anhydrous methanol is delivered to the methanol vaporizer 15 through the liquid methanol delivery branch pipe 13 to vaporize and form anhydrous methanol vapor. Then, it is delivered to the first methanol vapor delivery pipe 2 through the buffer tank 16, heated by the compressor 4, and then superheated by the heat exchanger 5 before being delivered to the sodium methoxide synthesis tower 1 to participate in the synthesis of sodium methoxide. The top of the sodium methoxide synthesis tower 1 delivers tail gas to the distillation tower 7 through the tail gas delivery pipe 3. The tail gas enters the sodium methoxide synthesis tower 1 to form a first upward gas flow. The first upward gas flow is delivered to the heat source channel of the top condenser 8 through the third packing layer 30 and the medium in the cold source channel of the top condenser 8 to exchange heat and form condensate. The condensate is then cooled by the top condenser 8. The source channel is returned to the distillation column 7 to form the first reflux condensate. The first reflux condensate and the first rising gas flow exchange heat countercurrently in the third packing layer 30. The methanol component in the first reflux condensate is evaporated and rises with the first rising gas flow, thereby increasing the methanol content in the first rising gas flow. The water component in the first rising liquid flow is liquefied and transported with the first reflux condensate through the third packing layer 30 to the second packing layer 29 as the second reflux condensate. During this period, the second part of anhydrous methanol is continuously transported to the cold source channel of the top condenser 8 through the liquid methanol transport main pipe 12, serving as the medium in the cold source and heat source channel of the top condenser 8 for heat exchange. The outlet end of the cold source channel of the top condenser 8 continuously transports vaporized anhydrous methanol vapor to the buffer tank 16 and merges it into the methanol vapor vaporized by the methanol vaporizer 15.

[0025] S2. When the flow parameter fed back by the first gas flow sensor 20 reaches the preset range, the continuous supply of anhydrous methanol solution to the methanol vaporizer 15 can be stopped. During this period, the outlet end of the heat source channel of the tower top condenser 8 continuously supplies process gas to the adsorption tank 9 in the working state to remove moisture and form a regenerated anhydrous methanol gas flow. This gas flow is then transported to the buffer tank 16 and merged into the vaporized anhydrous methanol vapor that is continuously supplied to the buffer tank 16 from the outlet end of the cold source channel of the tower top condenser 8. This vaporized methanol vapor forms a part of the anhydrous methanol gas flow that is supplied to the sodium methoxide synthesis tower 1 through the first methanol vapor transport pipe 2. During this period, the second reflux condensate continuously passes through the second packing layer 29 to the top of the baffle 28 and is then transported to the first circulation pipe 32. The liquid medium received by the first circulation pipe 32 is divided into two parts: a first part of reflux liquid and a second part of reflux liquid. The first part of reflux liquid is transported to the first packing layer 26 via the condensate delivery pipe 34 and the reflux nozzle 27 to form a third reflux condensate. The second part of reflux liquid then passes through the first reboiler 36 to form a first gas-liquid mixture. After the first gas-liquid mixture is returned to the distillation column 7 between the second packing layer 29 and the third packing layer 30, the gas phase portion of the first gas-liquid mixture is merged into the first rising gas flow, and the liquid phase portion of the first gas-liquid mixture is merged into the second reflux condensate.

[0026] S3. As the flow parameter fed back by the third gas flow sensor 45 gradually increases, the flow rate of anhydrous methanol supplied to the cold source channel of the top condenser 8 through the liquid methanol delivery main pipe 12 should be gradually reduced so that the flow parameter of the second gas flow sensor 21 is always maintained within the preset range. At the same time, the third reflux condensate descends to the bottom of the distillation column 7 and enters the second circulation pipe 38. Driven by the third circulation pump 40 and the second reboiler 43, it forms a second gas-liquid mixture. The second gas-liquid mixture is sent back through the outlet end of the second circulation pipe 38. In the distillation column 7 below the first packing layer 26, the gas phase portion of the second gas-liquid mixture moves toward the first packing layer 26 to form a third upward gas flow. The third upward gas flow and the third reflux condensate exchange heat countercurrently in the first packing layer 26. The water component in the third upward gas flow is liquefied and transported to the bottom of the distillation column 7 along with the third reflux condensate. The liquid at the bottom of the distillation column 7 is then combined and transported to the second circulation pipe 38. The liquid phase portion of the second gas-liquid mixture is then transported to the bottom of the distillation column 7 and combined with the liquid at the bottom of the distillation column 7.

[0027] The methanol component in the third reflux condensate is vaporized and merged into the third rising gas stream. It then ascends along with the third rising gas stream, passing through several riser caps 31 to form a second rising gas stream, which is delivered to the second packing layer 29 and undergoes countercurrent heat exchange with the second reflux condensate continuously supplied to the second packing layer 29. The methanol component in the second reflux condensate is vaporized and merges into the first rising gas stream after passing through the second packing layer 29 with the second rising gas stream. The water component in the second rising gas stream is liquefied and descends along with the second reflux condensate, continuously supplied to the first circulation pipe 32. This forms a distillation system for the tail gas supplied by the tail gas delivery pipe 3 to the distillation column 7. This results in a continuous supply of low-moisture methanol vapor to the adsorption tank 9, which is in operation, via the heat source channels at the top of the distillation column 7 and the top condenser 8, thereby reducing the frequency of desorption during the regeneration of the molecular sieve layer 10 in the adsorption tank 9.

[0028] It should be noted that the liquid at the bottom of the distillation column 7 is a liquid with a low methanol content. When the parameters fed back by the second online chromatograph 39 reach the preset range, they should be discharged in time to increase the methanol content of the liquid at the bottom of the distillation column 7, so that the methanol component in the third rising gas stream is always maintained within the preset range.

[0029] In this embodiment, the product reduces the water content in the tail gas after distillation in the distillation column 7, forming a gas to be adsorbed, which is then transported to the adsorption tank 9 in operation. Under the adsorption of the molecular sieve layer 10 in the adsorption tank 9, anhydrous methanol gas is formed and sent back to the sodium methoxide synthesis tower 1 to participate in the synthesis of sodium methoxide. This solves the technical difficulty of not being able to obtain anhydrous methanol vapor by simply using distillation, and also reduces the technical problem of excessively high frequency of molecular sieve desorption and regeneration due to the high water content in the tail gas when simply using molecular sieve adsorption. It is worthy of promotion and application.

[0030] The embodiments described above are merely preferred embodiments of this utility model and are not intended to limit the scope of implementation of this utility model. Therefore, all equivalent changes or modifications made to the structure, features and principles described in the patent claims of this utility model should be included within the scope of the patent application of this utility model.

Claims

1. A methanol vapor recovery and utilization device for producing sodium methoxide, comprising a sodium methoxide synthesis tower (1), wherein the sodium methoxide synthesis tower (1) is provided with a first methanol vapor conveying pipe (2) and a tail gas conveying pipe (3), characterized in that: The first methanol vapor conveying pipe (2) is provided with a compressor (4), a superheater (5), and a first regulating valve (6) in sequence along the direction away from the sodium methoxide synthesis tower (1) and closer to the sodium methoxide synthesis tower (1). A distillation tower (7) is provided on the tail gas conveying pipe (3). A top condenser (8) is provided at the top of the distillation tower (7). The heat source channel of the top condenser (8) is connected to the inner cavity of the distillation tower (7). The top end of the heat source channel of the top condenser (8) is connected to an adsorption tank (9). A molecular sieve layer (10) is provided inside the adsorption tank (9). The inlet end of the second methanol vapor transmission pipe (11) is provided, the inlet end of the heat source channel of the tower top condenser (8) is provided with a liquid methanol transmission main pipe (12), the liquid methanol transmission main pipe (12) is provided with a liquid methanol transmission branch pipe (13), the liquid methanol transmission branch pipe (13) is provided with a first shut-off valve (14) and the inlet end of the methanol vaporizer (15), the outlet end of the methanol vaporizer (15), the second methanol vapor transmission pipe (11), the outlet end of the heat source channel of the tower top condenser (8) and the first methanol vapor transmission pipe (2) are provided with a buffer tank (16).

2. The methanol vapor recovery and utilization device for producing sodium methoxide according to claim 1, characterized in that: The liquid methanol delivery main pipe (12) is provided with a liquid flow sensor (17), a second regulating valve (18) and a first booster pump (19) in sequence along the direction from near the top condenser (8) to away from the top condenser (8). A first gas flow sensor (20) is provided on the tail gas delivery pipe (3). A second gas flow sensor (21) is provided on the first methanol vapor delivery pipe (2) between the first regulating valve (6) and the sodium methoxide synthesis tower (1).

3. The methanol vapor recovery and utilization device for producing sodium methoxide according to claim 1, characterized in that: The second methanol vapor delivery pipe (11) is equipped with a first online chromatograph (22).

4. The methanol vapor recovery and utilization device for producing sodium methoxide according to claim 1, characterized in that: The number of adsorption tanks (9) is at least two. Each adsorption tank (9) is equipped with a molecular sieve layer (10). The outlet end of a first conveying pipe (23) is provided at the inlet end of each adsorption tank (9). The inlet ends of several first conveying pipes (23) are connected to the top of the heat source channel of the tower top condenser (8). The inlet end of a second conveying pipe (24) is provided at the outlet end of each adsorption tank (9). The outlet ends of several second conveying pipes (24) are connected to the inlet end of a second methanol vapor conveying pipe (11). A second shut-off valve (25) is provided on several second conveying pipes (24) and several first conveying pipes (23).

5. The methanol vapor recovery and utilization device for producing sodium methoxide according to claim 1, characterized in that: The distillation column (7) is provided with a first packing layer (26), a reflux nozzle (27), a baffle (28), a second packing layer (29), and a third packing layer (30) arranged sequentially from bottom to top in the inner cavity. Several gas lift caps (31) are provided on the baffle (28). The distillation column (7) between the second packing layer (29) and the third packing layer (30) is connected to the outlet end of the tail gas delivery pipe (3). The distillation column (7) between the baffle (28) and the second packing layer (29), as well as the second packing layer (29) and... The distillation column (7) of the third packing layer (30) is provided with a first circulation pipe (32). Along the direction from the inlet end of the first circulation pipe (32) to the outlet end of the first circulation pipe (32), a second booster pump (33), the inlet end of the condensate delivery pipe (34), a third regulating valve (35) and a first reboiler (36) are arranged in sequence. A fourth regulating valve (37) is provided on the condensate delivery pipe (34). The outlet end of the condensate delivery pipe (34) is connected to the inlet end of the reflux nozzle (27).

6. The methanol vapor recovery and utilization device for producing sodium methoxide according to claim 5, characterized in that: A second circulation pipe (38) is provided on the distillation column (7) below the third packing layer (30). The outlet end of the second circulation pipe (38) is located below the inlet end of the second circulation pipe (38). Along the direction from the inlet end of the second circulation pipe (38) to the outlet end of the second circulation pipe (38), a second online chromatograph (39), a third circulation pump (40), the inlet end of the waste liquid discharge pipe (41), a fifth regulating valve (42), and a second reboiler (43) are arranged in sequence. A sixth regulating valve (44) is provided on the waste liquid discharge pipe (41).

Images