Triethanolamine production device

Abstract

The invention discloses a triethanolamine production device, which belongs to the field of industrial production of chemicals, and is characterized in that the device comprises a reaction device and a separation device, the reaction device comprises a feed mixer, a first reactor, a reaction circulating pump, a reaction cooler, an interstage cooler, a second reactor, a tail gas absorption tank and a spray circulating pump. The separation device comprises a flash tank, a flash tank top condenser, a triethanolamine refining tower, a condenser, a reboiler, a reflux tank, a reflux pump and a circulating pump. On the basis of the traditional triethanolamine production process, the kettle type reactor is adopted, the reaction feeding ratio is controlled, and the reaction process is simplified, so that higher triethanolamine yield and lower production energy consumption are achieved.

Description

Technical Field

[0001] The invention belongs to the field of industrial production of chemical products, and in particular relates to a triethanolamine production device. Background Art

[0002] Triethanolamine is a weakly alkaline chemical product that can be compounded with a variety of inorganic acids or organic acids and is widely used in fields such as detergents, metalworking fluids, and epoxy resin curing agents. In industrial production, liquid ammonia or ammonia water and ethylene oxide are often used as raw materials to react in a tubular reactor at 4.5-6.2MPa (G) to generate a mixed product of monoethanolamine, diethanolamine, and triethanolamine, and then undergo a series of distillation separations to obtain a triethanolamine product. In the production process, if a higher proportion of triethanolamine products is desired, the diethanolamine obtained by subsequent separation is often required to be returned to the reactor to continue the reaction to obtain triethanolamine. However, in this process, the reaction process is complicated, and there is a competitive pipeline for the reaction of diethanolamine, monoethanolamine, ammonia, and ethylene oxide, which results in a low ratio of diethanolamine converted to triethanolamine, and only about 35-55% can be converted per 1000kg of diethanolamine. In addition, due to the existence of this circulation process, the reactor load increases, the reaction temperature and reaction pressure are higher, the operation risk increases, and the subsequent separation energy consumption also increases.

[0003] Based on the existing industrial process, the present invention proposes a triethanolamine production device, which uses ethylene oxide and diethanolamine as raw materials, simplifies the reaction process, and produces triethanolamine in a kettle reactor. The conversion rate of diethanolamine can reach up to 99%, and the energy consumption required for subsequent separation is also lower. Summary of the invention

[0004] In order to solve the technical problems raised in the background technology, the present invention provides a triethanolamine production device, and the technical solution includes:

[0005] A triethanolamine production device, comprising a reaction device and a separation device, characterized in that:

[0006] The reaction device comprises a feed mixer, a first reactor, a reaction circulation pump, a reaction cooler, an interstage cooler, a second reactor, a tail gas absorption tank and a spray circulation pump;

[0007] The feed mixer is connected to two feeds through pipelines, namely the diethanolamine pipeline and the catalyst pipeline. Both the diethanolamine pipeline and the catalyst pipeline are provided with emergency shut-off valves and flow regulating valves. A 90° right-angle nozzle is arranged inside the feed mixer 24. A plurality of elliptical small holes are evenly distributed along the fluid direction at the horizontal end of the nozzle. The opening direction of the small holes is at an angle of 30° to the horizontal direction.

[0008] The top of the first reactor is connected to a nitrogen pipeline, which is used to replace air in the reactor and to increase the pressure when the reactor is started. An emergency shut-off valve and a manual regulating valve are provided on the nitrogen pipeline. The first reactor includes a motor, a feed distributor, a stirring shaft, a feed extension pipe, an anti-vortex plate, a jacket cooling pipe, a stirring paddle and an anti-collision plate. The feed distributor 502 is an annular distributor with small holes evenly distributed at the bottom for dispersing ethylene oxide. The feed extension pipe 504 is connected to the feed mixer 24 to ensure that the material enters below the liquid level to prevent the reaction from being too intense and causing the reactor to overheat and overpressure. The anti-collision plate 508 is arranged at the circulation inlet to prevent the circulating material from impacting the stirring shaft. The anti-vortex plate is arranged at the bottom discharge port of the first reactor 5 to prevent vortexes;

[0009] The top of the first reactor is connected to the tail gas absorption tank through a pipeline, and an emergency shut-off valve and a reactor pressure regulating valve are arranged on the connected pipeline;

[0010] The bottom of the first reactor is connected to the inlet of a reaction circulation pump, and the outlet of the reaction circulation pump is connected to a reactor cooler;

[0011] Another outlet of the reaction circulation pump is connected to the interstage cooler, and a liquid level control regulating valve is arranged on the pipeline;

[0012] One outlet of the spray circulation pump is connected to the tail gas absorption tank for circulating spraying to absorb organic matter in the tail gas, and the other outlet is connected to the wastewater pipeline to be sent outside the device for treatment. The wastewater pipeline is equipped with a liquid level control regulating valve;

[0013] The separation device includes a flash tank, a flash tank top condenser, a triethanolamine refining tower, a condenser, a reboiler, a reflux tank, a reflux pump and a tower circulating pump. A metal wire mesh demister is arranged inside the flash tank 10, and the triethanolamine refining tower is a packed tower.

[0014] The top of the flash tank is connected to the flash tank top condenser through a pipeline, the bottom of the flash tank is connected to the triethanolamine refining tower through a pipeline, the top of the triethanolamine refining tower is connected to the condenser through a pipeline, the condenser is connected to the reflux tank through a pipeline, the reflux tank is connected to the reflux pump through a pipeline, and the reflux pump is connected to the circulating diethanolamine pipeline;

[0015] The bottom of the triethanolamine refining tower is connected to the reboiler and the tower bottom circulation pump through pipelines, and the tower bottom circulation pump is connected to the triethanolamine product pipeline.

[0016] The bottom of the second reactor receives the material from the interstage cooler, the top of the second reactor is connected to the flash tank through a pipeline, a pressure regulating valve is arranged on the connected pipeline, and four thermometers are evenly arranged from top to bottom in the second reactor.

[0017] The second reactor comprises a fixed plate, a cooling coil, a fixed rod and a spoiler. The fixed plate is welded to the inner wall of the second reactor, the fixed rod is connected to the fixed plate, the spoiler is inserted on the fixed rod in an alternating manner, and the cooling coil is evenly wound on the outer wall of the second reactor for emergency cooling.

[0018] The outlet of the reaction circulation pump is connected to the reactor cooler, and the heat released by the reaction process is absorbed by 30°C circulating water.

[0019] The reaction cooler can be switched to 72-85°C hot water to heat the reactor when the first reactor is started. Another outlet of the reactor circulation pump is connected to the interstage cooler, and a liquid level control regulating valve is set on the pipeline. The interstage cooler uses 30°C circulating water to reduce the discharge temperature of the first reactor and then send it to the second reactor.

[0020] The present invention has the following advantages:

[0021] The triethanolamine production device provided by the present invention adopts a kettle reactor, uses ethylene oxide and diethanolamine as raw materials, and has a higher conversion rate of triethanolamine. At the same time, due to the reduction of by-product content, the subsequent separation process is shorter and the energy consumption required for the entire separation process is lower. BRIEF DESCRIPTION OF THE DRAWINGS

[0022] Figure 1 It is a flow chart of the present invention.

[0023] Figure 2 This is a cross-sectional view of the first reactor.

[0024] Figure 3 This is a cross-sectional view of the second reactor.

[0025] Figure 4 Schematic diagram of the nozzle in the feed mixer.

[0026] In the figure: 1, nitrogen pipeline, 2, ethylene oxide pipeline, 3, diethanolamine pipeline, 4 catalyst pipeline, 5, first reactor, 6, reaction cooler, 7, reaction circulation pump, 8, interstage cooler, 9, second reactor, 10, flash tank, 11, flash tank top condenser, 12, triethanolamine refining tower, 13, condenser, 14, reflux tank, 15, reflux pump, 16, circulating diethanolamine pipeline, 17, reboiler, 18, tower bottom circulation pump, 19, Triethanolamine product pipeline, 20. Tail gas absorption tank, 21. Spray circulation pump, 22. Waste water, 23. Circulating catalyst pipeline, 24. Feed mixer, 501. Motor, 502. Feed distributor, 503. Stirring shaft, 504. Feed extension pipe, 505. Anti-vortex plate, 506. Jacket cooling pipe, 507. Stirring paddle, 508. Anti-impact plate, 901. Fixed plate, 902. Cooling coil, 903. Fixed rod, 904. Spoiler. DETAILED DESCRIPTION

[0027] Example 1

[0028] like Figure 1-Figure 4 As shown:

[0029] A triethanolamine production device comprises a reaction device and a separation device.

[0030] The reaction device includes a feed mixer 24, a first reactor 5, a reaction circulation pump 7, a reaction cooler 6, an interstage cooler 8, a second reactor 9, a tail gas absorption tank 20 and a spray circulation pump 21. A 90° right-angle nozzle is arranged inside the feed mixer 24. A plurality of elliptical small holes are evenly distributed along the fluid direction at the horizontal end of the nozzle. The opening direction of the small holes forms an angle of 30° with the horizontal direction.

[0031] The first reactor 5 includes a motor 501, a feed distributor 502, a stirring shaft 503, a feed extension pipe 504, an anti-vortex plate 505, a jacket cooling pipe 506, a stirring paddle 507 and an anti-collision plate 508. The feed distributor 502 is an annular distributor with small holes evenly distributed at the bottom for dispersing ethylene oxide. The feed extension pipe 504 is connected to the feed mixer 24 to ensure that the material enters below the liquid level to prevent the reaction from being too intense and causing the reactor to overheat and overpressure. The anti-collision plate 508 is arranged at the circulation inlet to prevent the circulating material from impacting the stirring shaft. The anti-vortex plate is arranged at the bottom discharge port of the first reactor 5 to prevent vortexes.

[0032] The feed mixer 24 is connected to two feeds through pipelines, namely the diethanolamine pipeline 2 and the catalyst pipeline 4. Both the diethanolamine pipeline 2 and the catalyst pipeline 4 are provided with an emergency shut-off valve and a flow regulating valve;

[0033] The top of the first reactor 5 is connected to a nitrogen pipeline 1, and nitrogen is used to replace air in the reactor and to increase the pressure during startup. An emergency shut-off valve and a manual regulating valve are provided on the nitrogen pipeline 1. The top of the first reactor 5 is connected to the tail gas absorption tank 20 through a pipeline, and an emergency shut-off valve and a reactor pressure regulating valve are provided on the connected pipeline. The bottom of the first reactor 5 is connected to the inlet of a reaction circulation pump 7, and the outlet of the reaction circulation pump 7 is connected to a reactor cooler 6. Another outlet of the reaction circulation pump 7 is connected to an interstage cooler 8, and a liquid level control regulating valve is provided on the pipeline.

[0034] One outlet of the spray circulation pump 21 is connected to the tail gas absorption tank 20 for circulating spraying to absorb organic matter in the tail gas, and the other outlet is connected to the wastewater pipeline 22 for external treatment. The wastewater pipeline 22 is provided with a liquid level control regulating valve.

[0035] The separation device includes a flash tank 10, a flash tank top condenser 11, a triethanolamine refining tower 12, a condenser 13, a reboiler 17, a reflux tank 14, a reflux pump 15 and a tower circulating pump 16.

[0036] The top of the flash tank 10 is connected to the flash tank top condenser 11 through a pipeline, a wire mesh demister is arranged inside the flash tank 10, the bottom of the flash tank 10 is connected to the triethanolamine refining tower 12 through a pipeline, the top of the triethanolamine refining tower 12 is connected to the condenser 13 through a pipeline, the triethanolamine refining tower 12 is a packed tower, the condenser 13 is connected to the reflux tank 14 through a pipeline, the reflux tank 14 is connected to the reflux pump 15 through a pipeline, and the reflux pump 15 is connected to the circulating diethanolamine pipeline 16.

[0037] The bottom of the triethanolamine refining tower 12 is connected to the reboiler 17 and the tower bottom circulation pump 18 through pipelines, and the tower bottom circulation pump 18 is connected to the triethanolamine product pipeline 19.

[0038] The bottom of the second reactor 9 receives the material from the interstage cooler 8, and the top of the second reactor 9 is connected to the flash tank 10 through a pipeline. A pressure regulating valve is arranged on the connected pipeline. Four thermometers are evenly arranged from top to bottom of the second reactor 9.

[0039] The second reactor 9 comprises a fixing plate 901, a cooling coil 902, a fixing rod 903 and a spoiler 904. The fixing plate 901 is welded to the inner wall of the second reactor 9, the fixing rod 903 is connected to the fixing plate 901, the spoiler 904 is staggeredly inserted on the fixing rod 903, and the cooling coil 902 is evenly wound on the outer wall of the second reactor 9 for emergency cooling.

[0040] The workflow of the present invention is as follows:

[0041] (1) The air in the first reactor 5 and the second reactor 9 is replaced by nitrogen and the pressure is increased. The pressure of the first reactor is controlled by the gas phase regulating valve at the top.

[0042] (2) The reaction raw materials diethanolamine 3 and catalyst 4 are piped to the feed mixer, and after premixing, they enter the bottom of the first reactor 5, and ethylene oxide 2 is added to the first reactor 5 from the middle. The materials in the reactor are circulated through the reaction circulation pump 7, and the reaction cooler 6 first passes 72-85°C hot water to heat the materials until the reaction begins. When the first reactor 5 starts to heat up, the reaction cooler 6 is changed to 30°C circulating water to cool the materials. After the reaction, the material at the bottom of the first reactor 5 is a mixture of diethanolamine, triethanolamine, water and a small amount of ethylene oxide.

[0043] (3) After the reaction in the first reactor 5, the mixed material enters the second reactor 9 from the bottom to continue the reaction. The reaction ensures that the ethylene oxide is completely consumed, and then enters the flash tank 10 for flash evaporation. Most of the water and a small amount of diethanolamine flashed out are condensed by the flash tank top condenser 11 and then recovered to the first reactor 5.

[0044] (4) The material at the bottom of the flash tank 10 enters the triethanolamine refining tower 12 from the middle, and the light impurities including water and diethanolamine are separated from the top of the tower through rectification. A triethanolamine product with a purity of 99.3% (mass fraction) is extracted from the bottom of the tower.

[0045] Implementation Case 1:

[0046] The feed rate of diethanolamine is 2.4 t / h, the feed rate of ethylene oxide is 1 t / h, and the feed rate of catalyst is 10 kg / h.

[0047] The first reactor 5 is replaced with nitrogen to increase the pressure. The oxygen content in the first reactor 5 needs to be lower than 0.02%. The pressure of the first reactor 5 is increased to 3 MPa (G).

[0048] After mixing, diethanolamine and the catalyst enter the bottom of the first reactor 5, start the reaction circulation pump 7, and heat it to 52°C with hot water through the reaction cooler 6, and add ethylene oxide. When the temperature of the first reactor 5 rises to 105°C, the reaction cooler 6 switches to 30°C circulating water to cool the reactor to ensure that the reactor temperature is controlled at 93°C. During the reaction, the pressure of the reactor is controlled at 3.0MPa (G) by controlling the gas phase amount of the tail gas absorption tower at the top of the first reactor 5. The tail gas generated during the reaction is absorbed by water and discharged at a high point after reaching the standard.

[0049] The discharge from the first reactor 5 is cooled to 80°C by the interstage cooler 8, enters the second reactor 9 from the bottom, and is discharged from the top of the second reactor 9; 4 thermometers are evenly arranged from top to bottom in the second reactor 9, and the top temperature shall not be higher than the three temperatures below.

[0050] The discharge from the top of the second reactor 9 enters the flash tank 10 for flash evaporation. The flashed gas phase comprises water and a small amount of diethanolamine. After being cooled at the top of the flash tank, it is circulated to the first reactor 5 as a catalyst. The liquid phase material at the bottom of the flash tank 10 is sent to the triethanolamine refining tower 12 through the static pressure difference. The pressure of the flash tank 10 is controlled at 0.1 MPa (G).

[0051] The gas phase at the top of the triethanolamine refining tower 12 is condensed and enters the reflux tank 14, and then a part of it is transported to the top of the tower by the reflux pump 15 as reflux, and the other part is returned to the first reactor 5 as a reaction raw material. The liquid phase in the tower bottom is returned to the bottom of the tower after being heated by the reboiler 17 through the tower bottom circulation pump 16, and the other part is produced as the triethanolamine product. The triethanolamine refining tower 12 is a negative pressure tower, and the pressure is controlled at 0.1KPa (A). The tower top temperature is controlled at 103°C, and the tower bottom temperature is controlled at 183°C. The tower top reflux volume is 1.2t / h, the tower top production volume is 2.1t / h, and the tower bottom produces 2.8t / h of triethanolamine with a purity of ≥99.3% (mass fraction). The steam consumption in the tower is 2.4t / h.

[0052] Implementation Case 2:

[0053] The feed rate of diethanolamine is 6 t / h, the feed rate of ethylene oxide is 1 t / h, and the feed rate of catalyst is 500 kg / h.

[0054] The first reactor 5 is replaced with nitrogen to increase the pressure. The oxygen content in the first reactor 5 needs to be lower than 0.02%. The pressure of the first reactor 5 is increased to 5.2 MPa (G).

[0055] After mixing, diethanolamine and the catalyst enter the bottom of the first reactor 5, start the reaction circulation pump 7, and heat it to 73°C with hot water through the reaction cooler 6, and add ethylene oxide. When the temperature of the first reactor 5 rises to 105°C, the reaction cooler 6 switches to 30°C circulating water to cool the reactor to ensure that the reactor temperature is controlled at 116°C. During the reaction, the pressure of the reactor is controlled at 5.2MPa(G) by controlling the gas phase amount of the tail gas absorption tower at the top of the first reactor 5. The tail gas generated during the reaction is absorbed by water and discharged at a high point after reaching the standard.

[0056] The discharge from the first reactor 5 is cooled to 95°C by the interstage cooler 8, enters the second reactor 9 from the bottom, and is discharged from the top of the second reactor 9; 4 thermometers are evenly arranged from top to bottom in the second reactor 9, and the top temperature shall not be higher than the three temperatures below.

[0057] The discharge from the top of the second reactor 9 enters the flash tank 10 for flash evaporation. The flashed gas phase comprises water and a small amount of diethanolamine. After being cooled at the top of the flash tank, it is circulated to the first reactor 5 as a catalyst. The liquid phase material at the bottom of the flash tank 10 is sent to the triethanolamine refining tower 12 through the static pressure difference. The pressure of the flash tank 10 is controlled at 0.23 MPa (G).

[0058] The gas phase at the top of the triethanolamine refining tower 12 is condensed and enters the reflux tank 14, and then a part of it is transported to the top of the tower by the reflux pump 15 as reflux, and the other part is returned to the first reactor 5 as a reaction raw material. The liquid phase in the tower bottom is returned to the bottom of the tower after being heated by the reboiler 17 through the tower bottom circulation pump 16, and the other part is produced as the triethanolamine product. The triethanolamine refining tower 12 is a negative pressure tower, and the pressure is controlled at 0.6KPa (A). The tower top temperature is controlled at 126℃, and the tower bottom temperature is controlled at 206℃. The tower top reflux rate is 1.2t / h, the tower top production rate is 3.6t / h, and the tower bottom produces 3.0t / h of triethanolamine with a purity of ≥99.0% (mass fraction). The steam consumption in the tower is 3.5t / h.

[0059] Implementation Case 3:

[0060] The feed rate of diethanolamine is 4.77 t / h, the feed rate of ethylene oxide is 1 t / h, and the feed rate of catalyst is 100 kg / h.

[0061] The first reactor 5 is replaced with nitrogen to increase the pressure. The oxygen content in the first reactor 5 needs to be lower than 0.02%. The pressure of the first reactor 5 is increased to 4.5 MPa (G).

[0062] After mixing, diethanolamine and the catalyst enter the bottom of the first reactor 5, start the reaction circulation pump 7, and heat it to 73°C with hot water through the reaction cooler 6, and add ethylene oxide. When the temperature of the first reactor 5 rises to 105°C, the reaction cooler 6 switches to 30°C circulating water to cool the reactor to ensure that the reactor temperature is controlled at 110°C. During the reaction, the pressure of the reactor is controlled at 4.5MPa(G) by controlling the gas phase amount of the tail gas absorption tower at the top of the first reactor 5. The tail gas generated during the reaction is absorbed by water and discharged at a high point after reaching the standard.

[0063] The discharge from the first reactor 5 is cooled to 85°C by the interstage cooler 8, enters the second reactor 9 from the bottom, and is discharged from the top of the second reactor 9; 4 thermometers are evenly arranged from top to bottom in the second reactor 9, and the top temperature shall not be higher than the three temperatures below.

[0064] The discharge from the top of the second reactor 9 enters the flash tank 10 for flash evaporation. The flashed gas phase comprises water and a small amount of diethanolamine. After being cooled at the top of the flash tank, it is circulated to the first reactor 5 as a catalyst. The liquid phase material at the bottom of the flash tank 10 is sent to the triethanolamine refining tower 12 through the static pressure difference. The pressure of the flash tank 10 is controlled at 0.15 MPa (G).

[0065] The gas phase at the top of the triethanolamine refining tower 12 is condensed and enters the reflux tank 14, and then a part of it is transported to the top of the tower by the reflux pump 15 as reflux, and the other part is returned to the first reactor 5 as a reaction raw material. The liquid phase in the tower bottom is returned to the bottom of the tower after being heated by the reboiler 17 through the tower bottom circulation pump 16, and the other part is produced as the triethanolamine product. The triethanolamine refining tower 12 is a negative pressure tower, and the pressure is controlled at 0.3KPa (A). The tower top temperature is controlled at 115°C, and the tower bottom temperature is controlled at 198°C. The tower top reflux volume is 1.2t / h, the tower top production volume is 2.4t / h, and the tower bottom produces 3.3t / h of triethanolamine with a purity of ≥99.7% (mass fraction). The steam consumption in the tower is 2.6t / h.

[0066] When the ethylene oxide feed rate is 1t / h, the prior art is compared with the above cases, and the comparison data are as follows:

[0067]

Claims

1. A triethanolamine production device, comprising a reaction device and a separation device, characterized in that: The reaction device comprises a feed mixer (24), a first reactor (5), a reaction circulation pump (7), a reaction cooler (6), an interstage cooler (8), a second reactor (9), a tail gas absorption tank (20) and a spray circulation pump (21); The feed mixer (24) is connected to two feeds through pipelines, namely a diethanolamine pipeline (3) and a catalyst pipeline (4). Both the diethanolamine pipeline (3) and the catalyst feed pipeline (4) are provided with an emergency shut-off valve and a flow regulating valve; The top of the first reactor (5) is connected to a nitrogen pipeline (1), and the nitrogen pipeline (1) is provided with an emergency shut-off valve and a manual regulating valve; The top of the first reactor (5) is connected to the tail gas absorption tank (20) via a pipeline, and an emergency shut-off valve and a reactor pressure regulating valve are arranged on the connected pipeline; The bottom of the first reactor (5) is connected to the inlet of a reaction circulation pump (7), and the outlet of the reaction circulation pump (7) is connected to a reactor cooler (6); Another outlet of the reaction circulation pump (7) is connected to the interstage cooler (8), and a liquid level control regulating valve is arranged on the pipeline; One outlet of the spray circulation pump (21) is connected to the tail gas absorption tank (20) for circulating spraying to absorb organic matter in the tail gas, and the other outlet is connected to the waste water pipeline (22) to be sent to the outside of the device for treatment. The waste water pipeline (22) is provided with a liquid level control regulating valve; The separation device comprises a flash tank (10), a flash tank top condenser (11), a triethanolamine refining tower (12), a condenser (13), a reboiler (17), a reflux tank (14), a reflux pump (15) and a tower circulating pump (16); The top of the flash tank (10) is connected to the flash tank top condenser (11) through a pipeline, the bottom of the flash tank (10) is connected to the triethanolamine refining tower (12) through a pipeline, the top of the triethanolamine refining tower (12) is connected to the condenser (13) through a pipeline, the condenser (13) is connected to the reflux tank (14) through a pipeline, the reflux tank (14) is connected to the reflux pump (15) through a pipeline, and the reflux pump (15) is connected to the circulating diethanolamine pipeline (16); The bottom of the triethanolamine refining tower (12) is connected to the reboiler (17) and the tower bottom circulation pump (18) through pipelines, and the tower bottom circulation pump (18) is connected to the triethanolamine product pipeline (19).

2. A triethanolamine production device as claimed in claim 1, characterized in that, The feed mixer (24) is provided with a 90° right-angle nozzle inside, and a plurality of elliptical small holes are evenly distributed along the fluid direction at the horizontal end of the nozzle, and the angle between the opening direction of the small holes and the horizontal direction is 30°.

3. A triethanolamine production device as claimed in claim 1, characterized in that, A metal wire mesh demister is arranged inside the flash tank (10).

4. A triethanolamine production device as claimed in claim 1, characterized in that, The triethanolamine refining tower (12) is a packed tower.

5. A triethanolamine production device as claimed in claim 1, characterized in that, The first reactor (5) comprises a motor (501), a feed distributor (502), a stirring shaft (503), a feed extension pipe (504), an anti-vortex plate (505), a jacket cooling pipe (506), a stirring paddle (507) and an anti-collision plate (508). The feed distributor (502) is an annular distributor with small holes evenly distributed at the bottom for dispersing ethylene oxide. The feed extension pipe (504) is connected to the feed mixer (24) to ensure that the material enters below the liquid surface to prevent the reaction from being too intense and causing the reactor to overheat and overpressure. The anti-collision plate (508) is arranged at the circulation inlet to prevent the circulating material from impacting the stirring shaft. The anti-vortex plate is arranged at the bottom discharge port of the first reactor (5) to prevent vortex.

6. A triethanolamine production device as claimed in claim 1, characterized in that: The bottom of the second reactor (9) receives the material from the interstage cooler (8), the top of the second reactor (9) is connected to the flash tank (10) through a pipeline, a pressure regulating valve is arranged on the connected pipeline, and four thermometers are evenly arranged from top to bottom in the second reactor (9).

7. A triethanolamine production device as claimed in claim 1, characterized in that: The second reactor (9) comprises a fixed plate (901), a cooling coil (902), a fixed rod (903) and a spoiler (904); the fixed plate (901) is welded to the inner wall of the second reactor (9); the fixed rod (903) is connected to the fixed plate (901); the spoiler (904) is staggered and inserted on the fixed rod (903); and the cooling coil (902) is evenly wound on the outer wall of the second reactor (9) for emergency cooling.

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