Epoxy sulfide steam stripping system

Abstract

The utility model discloses an epoxy thioether steam stripping system which comprises a gas-liquid separator, a steam stripping transfer kettle, a first condenser, a delivery pump, a steam stripping tower, a second condenser, a third condenser, an oil-water separator, a thioether receiving tank, an epoxy layering tank, a potassium salt water tank and an epoxy receiving tank, a first discharging opening of the gas-liquid separator is connected with a feeding opening of the steam stripping transfer kettle through a first conveying pipe, a liquid discharging opening of the steam stripping transfer kettle is connected with a feeding opening of the steam stripping tower through a second conveying pipe, and a discharging opening of the steam stripping tower is connected with the epoxy layering tank through a third conveying pipe; a supernatant outlet of the epoxy layering tank is connected with the epoxy receiving tank through a fourth conveying pipe, and a subnatant outlet of the epoxy layering tank is connected with the potassium salt water tank through a fifth conveying pipe; and an exhaust port of the stripping tower is connected with a gas inlet of the second condenser through a third condensation pipe. The steam stripping tower is high in steam stripping efficiency, high in thioether utilization rate, low in product impurity rate, stable in air pressure and high in operation efficiency.

Description

Technical Field

[0001] The utility model relates to the technical field of epoxy distillation thioether, in particular to an epoxy thioether stripping system. Background Art

[0002] Thioether is soluble in ethanol and ether, insoluble in water, a colorless, transparent and volatile liquid with an unpleasant smell. Epoxy thioether stripping is usually used to remove the dissolved thioether gas in epoxy. The principle is to introduce carrier gas such as water vapor into water, so that the carrier gas fully contacts with the wastewater, causing the dissolved gas and some volatile substances in epoxy to transfer to the gas phase, so as to achieve the purpose of removing impurities in epoxy. Generally, steam is used as the carrier gas. When reusing epoxy thioether, the thioether distillation kettle is prone to overpressure, the distillation efficiency is low, the distillation kettle is prone to material flushing and siphonage, resulting in premature crystallization of potassium salt to block the pipeline, incomplete removal of thioether, and high impurity content. Summary of the Utility Model

[0003] The utility model provides an epoxy thioether stripping system, which solves the problems that the traditional thioether distillation kettle is prone to overpressure, the stripping efficiency is low, the stripping of thioether is not clean, and the distillation kettle is prone to material flushing and siphonage.

[0004] The utility model provides an epoxy thioether stripping system, including a gas-liquid separator, a stripping transfer kettle, a first condenser, a transfer pump, a stripping tower, a second condenser, a third condenser, an oil-water separator, a thioether receiving tank, an epoxy stratification tank, a potassium salt water tank, and an epoxy receiving tank. The first discharge port of the gas-liquid separator is connected to the feeding port of the stripping transfer kettle through a first conveying pipe. The liquid discharge port of the stripping transfer kettle is connected to the feeding port of the stripping tower through a second conveying pipe, and a transfer pump is arranged on the second conveying pipe. The discharge port of the stripping tower is connected to the epoxy stratification tank through a third conveying pipe. The upper liquid outlet of the epoxy stratification tank is connected to the epoxy receiving tank through a fourth conveying pipe. The lower liquid outlet of the epoxy stratification tank is connected to the potassium salt water tank through a fifth conveying pipe. The exhaust port of the stripping tower is connected to the inlet of the second condenser through a third condenser pipe. The liquid outlet of the second condenser is connected to the liquid inlet of the oil-water separator through a fourth condenser pipe. The condensate gas outlet of the second condenser is connected to the condensate gas inlet of the third condenser through a fifth condenser pipe. The liquid outlet of the third condenser is connected to the liquid inlet of the oil-water separator through a sixth condenser pipe. The drain port of the oil-water separator is connected to the water inlet of the stripping tower through a sixth conveying pipe. The upper liquid outlet of the oil-water separator is connected to the thioether receiving tank through a seventh conveying pipe. The second discharge port of the gas-liquid separator is connected to the thioether receiving tank through an eighth conveying pipe.

[0005] In the above technical solution, further, the second exhaust port of the gas-liquid separator is connected to a first vent pipe, and the exhaust port of the third condenser is connected to a second vent pipe. Vent control valves are arranged at the ends of the first vent pipe and the second vent pipe.

[0006] In the above technical solution, further, the second vent pipe is connected to the oil-water separator through the first gas-phase balance pipe, the second vent pipe is connected to the sixth delivery pipe through the second gas-phase balance pipe, the second vent pipe is connected to the third delivery pipe through the third gas-phase balance pipe, the second vent pipe is connected to the epoxy stratification tank through the fourth gas-phase balance pipe, and the second vent pipe is connected to the fifth delivery pipe through the fifth gas-phase balance pipe.

[0007] In the above technical solution, further, the exhaust port of the stripping intermediate kettle is connected to the gas inlet of the first condenser through the first condensate pipe, and the gas outlet of the first condenser is connected to the condensate inlet of the gas-liquid separator through the second condensate pipe.

[0008] In the above technical solution, further, the water inlet of the stripping intermediate kettle is connected to the process water tank through a water supply pipe.

[0009] In the above technical solution, further, a nitrogen supply port is provided at the top of the stripping column and is connected to a nitrogen supply pipeline.

[0010] From the above technical solutions, it can be seen that the present utility model provides an epoxy sulfide stripping system.

[0011] Compared with the prior art, the beneficial effects of the present utility model are as follows:

[0012] In the present utility model, before stripping in the stripping column, the epoxy mixture is heated to evaporate a part of the sulfide. At the same time, the gas-phase pipeline of the stripping column is raised to give a gas buffer space. The gas-phase pipe on the water outlet pipeline of the stripping column is changed from the condenser to the sulfide vent main pipe, reducing the heating and evaporation of sulfide in the condenser by hot gas, reducing the loss of sulfide, and preventing the occurrence of siphon phenomenon. The stripping efficiency is high, the utilization rate of sulfide is high, the impurity content of the product after stripping is low, the air pressure of the stripping column is stable, the operation efficiency is high, and the safety is good. The hydrolysis reaction is carried out by pressurizing nitrogen replacement through the nitrogen supply port provided at the top of the stripping column, improving the stripping speed. At the same time, the system pressure is automatically balanced and adjusted to prevent the premature crystallization and blockage of the pipeline by potassium salt. BRIEF DESCRIPTION OF THE DRAWINGS

[0013] In order to more clearly illustrate the technical solutions of the present utility model, the drawings required for use in the implementation cases will be briefly introduced below. Obviously, for those of ordinary skill in the art, without creative efforts, other drawings can also be obtained based on these drawings.

[0014] Figure 1 It is a schematic diagram of the overall structure of an epoxy sulfide stripping system proposed by the present utility model;

[0015] Figure 2 It is a schematic diagram of the pipeline connection of the first condenser, gas-liquid separator, and stripping intermediate kettle of an epoxy sulfide stripping system proposed by the present utility model;

[0016] Figure 3 This is a schematic diagram of the process principle of a partial structure of an epoxy sulfide stripping system proposed by the present utility model.

[0017] In the figure:

[0018] 1 - Gas - liquid separator;

[0019] 2 - Stripping transfer kettle; 21 - Water supply pipe; 22 - Process water tank;

[0020] 3 - First condenser;

[0021] 4 - Transfer pump;

[0022] 5 - Stripping tower;

[0023] 6 - Second condenser;

[0024] 7 - Third condenser;

[0025] 8 - Oil - water separator;

[0026] 9 - Sulfide receiving tank;

[0027] 10 - Epoxy stratification tank;

[0028] 11 - Potassium salt water tank;

[0029] 12 - Epoxy receiving tank;

[0030] 101 - First transfer pipe; 102 - Second transfer pipe; 103 - Third transfer pipe; 104 - Fourth transfer pipe; 105 - Fifth transfer pipe; 106 - Sixth transfer pipe; 107 - Seventh transfer pipe; 108 - Eighth transfer pipe;

[0031] 201 - First condensing pipe; 202 - Second condensing pipe; 203 - Third condensing pipe; 204 - Fourth condensing pipe; 205 - Fifth condensing pipe; 206 - Sixth condensing pipe; 207 - First vent pipe; 208 - Second vent pipe;

[0032] 301 - First gas - phase equilibrium pipe; 302 - Second gas - phase equilibrium pipe; 303 - Third gas - phase equilibrium pipe; 304 - Fourth gas - phase equilibrium pipe; 305 - Fifth gas - phase equilibrium pipe. Detailed implementation manners

[0033] In order to enable those skilled in the art to better understand the technical solutions in the present utility model, the following will clearly and completely describe the technical solutions in the embodiments of the present utility model in conjunction with the drawings.

[0034] Example 1:

[0035] See Figures 1-3, An epoxy sulfide stripping system, comprising a gas-liquid separator 1, a stripping transfer kettle 2, a first condenser 3, a transfer pump 4, a stripping tower 5, a second condenser 6, a third condenser 7, an oil-water separator 8, a sulfide receiving tank 9, an epoxy stratification tank 10, a potassium salt water tank 11, and an epoxy receiving tank 12. The first discharge port provided at the bottom of the gas-liquid separator 1 is connected and communicated with the feeding port provided at the top of the stripping transfer kettle 2 through a first transfer pipe 101. The drain port provided at the bottom of the stripping transfer kettle 2 is connected and communicated with the feeding port provided on the side wall of the stripping tower 5 through a second transfer pipe 102. A transfer pump 4 is provided on the second transfer pipe 102. The discharge port provided at the bottom of the stripping tower 5 is connected and communicated with the epoxy stratification tank 10 through a third transfer pipe 103. The upper liquid outlet provided on the upper side wall of the epoxy stratification tank 10 is connected to the epoxy receiving tank 12 through a fourth transfer pipe 104. The lower liquid outlet provided on the lower side wall of the epoxy stratification tank 10 is connected to the potassium salt water tank 11 through a fifth transfer pipe 105. The exhaust port provided at the top of the stripping tower 5 is connected to the intake port provided at the top of the second condenser 6 through a third condensate pipe 203. The liquid outlet provided at the bottom of the second condenser 6 is connected to the liquid inlet of the oil-water separator 8 through a fourth condensate pipe 204. The condensate gas outlet provided at the top of the second condenser 6 is connected to the condensate gas inlet provided at the top of the third condenser 7 through a fifth condensate pipe 205. The liquid outlet provided at the bottom of the third condenser 7 is connected to the liquid inlet provided on the side wall of the oil-water separator 8 through a sixth condensate pipe 206. The drain port provided at the bottom of the oil-water separator 8 is connected to the water inlet provided in the middle of the stripping tower 5 through a sixth transfer pipe 106. The upper liquid outlet provided on the upper side wall of the oil-water separator 8 is connected to the sulfide receiving tank 9 through a seventh transfer pipe 107. The second discharge port provided at the bottom of the gas-liquid separator 1 is connected to the sulfide receiving tank 9 through an eighth transfer pipe 108. By heating and evaporating a part of the sulfide from the epoxy mixture before stripping in the stripping tower 5, and at the same time raising the gas-phase pipeline of the stripping tower 5 to give a gas buffer space, the gas-phase pipe on the water outlet pipeline of the stripping tower 5 is changed from the condenser to the sulfide vent main pipe, reducing the heating and evaporation of the sulfide in the condenser by the hot gas. Reducing the loss of sulfide, while preventing the occurrence of siphon phenomenon, high stripping efficiency, high utilization rate of sulfide, low impurity content in the product after stripping, stable operation efficiency of the stripping tower pressure, good safety, and the hydrolysis reaction is pressurized with nitrogen replacement through the nitrogen supply port provided at the top of the stripping tower 5, improving the stripping speed, and at the same time the system pressure realizes automatic balance adjustment to prevent the premature crystallization of potassium salt from blocking the pipeline.

[0036] In this embodiment, refer to Figure 1 , 3, the second exhaust port provided at the top of the gas-liquid separator 1 is connected to the first vent pipe 207, and the exhaust port provided at the top of the third condenser 7 is connected to the second vent pipe 208. Vent control valves are provided at the ends of the first vent pipe 207 and the second vent pipe 208. The gas emissions of the first vent pipe 207 and the second vent pipe 208 are controlled through the vent control valves to ensure that the air pressure inside the gas-liquid separator 1 and other equipment and pipelines remains balanced, preventing the occurrence of liquid siphon phenomenon.

[0037] In this embodiment, refer to Figure 1 , 3 , the second vent pipe 208 is connected to the oil-water separator 8 through the first gas-phase balance pipe 301, the second vent pipe 208 is connected to the sixth delivery pipe 106 through the second gas-phase balance pipe 302, the second vent pipe 208 is connected to the third delivery pipe 103 through the third gas-phase balance pipe 303, the second vent pipe 208 is connected to the epoxy stratification tank 10 through the fourth gas-phase balance pipe 304, and the second vent pipe 208 is connected to the fifth delivery pipe 105 through the fifth gas-phase balance pipe 305. The oil-water separator 8, the thioether receiving tank 9, the epoxy stratification tank 10, the potassium brine tank 11, and the epoxy receiving tank 12 are connected through the second vent pipe 208 to ensure that the air pressure inside each equipment remains consistent, realizing automatic pressure regulation and control, and ensuring the stability of the thioether gas system.

[0038] In this embodiment, refer to Figure 1 , 2 , the exhaust port of the stripping transfer kettle 2 is connected to the gas inlet of the first condenser 3 through the first condensate pipe 201, and the gas outlet of the first condenser 3 is connected to the condensate inlet of the gas-liquid separator 1 through the second condensate pipe 202.

[0039] In this embodiment, refer to Figure 1 , 2 , the water inlet of the stripping transfer kettle 2 is connected to the process water tank 22 through the water supply pipe 21.

[0040] In this embodiment, refer to Figure 1 , 2 , a nitrogen supply port is provided at the top of the stripping tower 5 and is connected to the nitrogen supply pipeline 109. The hydrolysis reaction is carried out by pressurizing with nitrogen through the nitrogen supply port provided at the top of the stripping tower 5 for nitrogen replacement.

[0041] In this embodiment, refer to Figure 1 , 2 , a transfer pump 4 is provided on the second delivery pipe 102. The liquid discharged from the stripping transfer kettle 2 is pressurized by the transfer pump 4 and quickly transported into the stripping tower 5, increasing the stripping efficiency.

[0042] In this embodiment, temperature sensors are provided at the top, middle, and bottom of the stripping column 5 to monitor the temperature inside the stripping column 5. The stripping column 5 is connected to a steam generator through a steam supply pipeline to supply steam to the middle and bottom of the stripping column 5. A flow meter and a flow control valve are provided on the steam supply pipeline to control the supply amount and supply speed of the steam, and a pressure gauge is also installed on the steam supply pipeline to monitor the pipeline pressure.

[0043] In this embodiment, a flow meter is installed on the second delivery pipe 102 to accurately control the liquid flow rate inside the second delivery pipe 102.

[0044] In this embodiment, heat exchange and condensation are carried out between the condensing gas and the circulating coolant introduced into the heat exchange chamber of the second condenser 6.

[0045] The working principle of the present utility model: The water and epoxy mixture are mixed in the stripping transfer kettle 2, heated to 50 - 60 °C for preliminary hydrolysis, and part of the thioether is evaporated and recovered by condensation through the first condenser 3 and collected in the thioether receiving tank 9. The remaining mixture is sent to the stripping column 5 for stripping; in the stripping column 5, steam and the epoxy mixture are mixed in the stripping column 5 for heat exchange and heated to 100 °C for sufficient hydrolysis of the material; a large amount of thioether gas is generated at the top of the column and enters the oil-water separator 8 after condensation through the second condenser 6 and the third condenser 7. The epoxy and potassium salt water generated after stripping at the bottom of the stripping column 5 enter the epoxy separation tank 10 along the pipeline for separation; in the oil-water separator 8, the upper layer is thioether and is collected in the thioether receiving tank 9, and the lower layer of steam water is recycled to the stripping column 5 to continue participating in hydrolysis; in the epoxy separation tank 10, the epoxy and potassium salt water are automatically separated here. The upper-layer liquid enters the epoxy receiving tank 12 through the fourth delivery pipe 104, and the lower-layer liquid enters the potassium salt water tank 11 through the fifth delivery pipe 105.

[0046] Those skilled in the art will readily think of other embodiments of the present utility model after considering the specification and practicing the utility model disclosed herein. The present utility model is intended to cover any variations, uses, or adaptations of the present utility model, which follow the general principles of the present utility model and include the common general knowledge or conventional technical means in the technical field not disclosed in the present utility model. The specification and examples are only regarded as exemplary, and the true scope of the present utility model is pointed out by the claims.

[0047] It should be understood that the present utility model is not limited to the precise structures already described and shown in the drawings, and various modifications and changes can be made without departing from its scope. The above-described embodiments of the present utility model do not constitute a limitation on the protection scope of the present utility model.

Claims

1. An epoxy sulfide stripping system, characterized in that: It includes a gas-liquid separator (1), a stripping transfer kettle (2), a first condenser (3), a transfer pump (4), a stripping tower (5), a second condenser (6), a third condenser (7), an oil-water separator (8), a thioether receiving tank (9), an epoxy stratification tank (10), a potassium salt water tank (11), and an epoxy receiving tank (12). The first discharge port of the gas-liquid separator (1) is connected to the feeding port of the stripping transfer kettle (2) through a first conveying pipe (101). The liquid discharge port of the stripping transfer kettle (2) is connected to the feeding port of the stripping tower (5) through a second conveying pipe (102). A transfer pump (4) is arranged on the second conveying pipe (102). The discharge port of the stripping tower (5) is connected to the epoxy stratification tank (10) through a third conveying pipe (103). The upper liquid outlet of the epoxy stratification tank (10) is connected to the epoxy receiving tank (12) through a fourth conveying pipe (104). The lower liquid outlet of the epoxy stratification tank (10) is connected to the potassium salt water tank (11) through a fifth conveying pipe (105). The exhaust port of the stripping tower (5) is connected to the air inlet of the second condenser (6) through a third condensing pipe (203). The liquid outlet of the second condenser (6) is connected to the liquid inlet of the oil-water separator (8) through a fourth condensing pipe (204). The condensed gas outlet of the second condenser (6) is connected to the condensed gas inlet of the third condenser (7) through a fifth condensing pipe (205). The liquid outlet of the third condenser (7) is connected to the liquid inlet of the oil-water separator (8) through a sixth condensing pipe (206). The drain port of the oil-water separator (8) is connected to the water inlet of the stripping tower (5) through a sixth conveying pipe (106). The upper liquid outlet of the oil-water separator (8) is connected to the thioether receiving tank (9) through a seventh conveying pipe (107). The second discharge port of the gas-liquid separator (1) is connected to the thioether receiving tank (9) through an eighth conveying pipe (108).

2. The epoxy sulfide stripping system according to claim 1, wherein The second exhaust port of the gas-liquid separator (1) is connected to a first vent pipe (207). The exhaust port of the third condenser (7) is connected to a second vent pipe (208). Vent control valves are arranged at the ends of the first vent pipe (207) and the second vent pipe (208).

3. The epoxy sulfide stripping system according to claim 2, characterized in that, The second vent pipe (208) is connected to the oil-water separator (8) through a first gas-phase balance pipe (301), connected to the sixth conveying pipe (106) through a second gas-phase balance pipe (302), connected to the third conveying pipe (103) through a third gas-phase balance pipe (303), connected to the epoxy stratification tank (10) through a fourth gas-phase balance pipe (304), and connected to the fifth conveying pipe (105) through a fifth gas-phase balance pipe (305).

4. An epoxy sulfide stripping system according to claim 1, characterized in that, The exhaust port of the stripping transfer kettle (2) is connected to the gas inlet of the first condenser (3) through the first condenser pipe (201), and the gas outlet of the first condenser (3) is connected to the condensate inlet of the gas-liquid separator (1) through the second condenser pipe (202).

5. The epoxy sulfide stripping system according to claim 1, characterized in that, The water inlet of the stripping transfer kettle (2) is connected to the process water tank (22) through the water supply pipe (21).

6. The epoxy sulfide stripping system according to claim 1, wherein A nitrogen supply port is arranged at the top of the stripping column (5) and is connected to the nitrogen supply pipeline (109).

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