CN201762266U - Trichloroethylene industrialized production device - Google Patents

Abstract

The utility model provides a trichloroethylene industrialized production device which adopts a structure as follows: an acetylene inlet pipeline and a chlorine inlet pipeline are respectively connected with the inlet end of a chlorination tower; the outlet end of a coarse tetrachloroethane tank is connected with the inlet end of a tetrachloroethane tower; the other outlet end of a dehydrochlorination reactor feed preheater is connected with the inlet end of a desorber; the outlet end of a resolution kettle liquid tank is connected with the inlet end of a low boiling tower; the outlet end at the lower part of the low boiling tower is connected with the inlet end of a low boiling tower reboiler and the inlet end of a trichloroethylene tower respectively; the outlet end of a trichloroethylene kettle liquid tank is connected with the inlet end of a middle distillate tower; the outlet end at the lower part of the middle distillate tower is connected with the inlet end of a middle distillate tower reboiler and the inlet end of the tetrachloroethylene tower respectively; and the heat exchangers of each complete condenser and each tail cooler adopt graphite pieces dipped with modified phenolic resin. The trichloroethylene industrialized production device has reasonable structure and high production capacity, and can run safely and stably for a long period. The produced trichloroethylene product has high quality.

Description

Trichlorethylene industrial production plant

technical field

The utility model provides an improved trichlorethylene production device.

Background technique

At present, the vast majority of domestic trichlorethylene production enterprises adopt the "gas-phase catalytic dehydrochlorination method" for production. Its simple production process is: chlorine gas and acetylene gas generate crude tetrachloroethane in the chlorination tower, the crude tetrachloroethane is vaporized after rectification, hydrogen chloride is removed in the dehydrochlorination reactor to generate trichloroethylene, and then through a A series of rectification operations produce qualified trichlorethylene products. Since the "gas-phase catalytic dehydrochlorination method" trichlorethylene production device is a new production process in recent years, other domestic trichlorethylene production enterprises have encountered a series of defects and problems in the operation process, which is manifested in the relatively small production capacity of the device , all about 10,000 tons/year, high energy consumption; small unit equipment load; poor comprehensive utilization of heat in the production device; difficult to solve the problem of medium corrosion in each process of the production device; the quality of trichlorethylene products is poor .

Contents of the invention

The technical problem to be solved by the utility model is to provide an industrial production device for trichlorethylene, which has a large production capacity and can run safely and stably for a long period.

The utility model is achieved in this way, the trichlorethylene industrial production device, it has the acetylene inlet pipeline and the chlorine gas inlet pipeline respectively connected with the inlet end of the chlorination tower, the outlet end of the chlorination tower is connected with the inlet end of the total condenser of the chlorination tower , the outlet of the chlorination tower full condenser is connected with the inlet of the chlorination reflux tank and the inlet of the tail cooler of the chlorination tower respectively, and the outlet of the tail cooler of the chlorination tower is connected with the inlet of the chlorination reflux tank and the inlet of the gas-liquid separator respectively , the outlet of the gas-liquid separator is connected to the inlet of the tail gas buffer tank, the outlet of the tail gas buffer tank is connected to the inlet of the hydraulic jet pump, the outlet of the hydraulic jet pump is connected to the inlet of the chlorination tail water tank, and the outlet of the chlorination tail water tank is connected to the chlorine The inlet of the chemical tailings tank is connected, the outlet of the chlorination tailings tank is connected to the inlet of the pressurized water pump, the outlet of the pressurized water pump is connected to the other inlet of the hydraulic jet pump, the outlet of the chlorination reflux tank is connected to the inlet of the crude tetrachloroethane tank The outlet of the crude tetrachloroethane tank is connected with the inlet of the tetrachloroethane tower, and the outlet of the lower part of the tetrachloroethane tower is connected with the inlet of the reboiler of the tetrachloroethane tower and the inlet of the refined tetrachloroethane tank respectively. connected, the tetrachloroethane tower reboiler outlet end is connected with the other inlet end of the tetrachloroethane tower, the outlet end of the tetrachloroethane tower top is connected with the tetrachloroethane tower full condenser inlet end, the tetrachloroethane The outlet of the total condenser of the tower is connected to the inlet of the reflux tank of the tetrachloroethane tower and the inlet of the tail cooler of the tetrachloroethane tower, and the outlet of the tail cooler of the tetrachloroethane is connected to the inlet of the reflux tank of the tetrachloroethane tower. The outlet of the refined tetrachloroethane tank is connected to the inlet of the tetrachloroethane vaporizer, the outlet of the tetrachloroethane vaporizer is connected to the inlet of the feed preheater of the dehydrochlorination reactor, and the outlet of the feed preheater of the dehydrochlorination reactor is It is connected to the inlet of the heat transfer oil preheater, the outlet of the heat transfer oil preheater is connected to the inlet of the dehydrochlorination reaction device, the outlet of the dehydrochlorination reaction device is connected to the other inlet of the feed preheater of the dehydrochlorination reactor, and the dehydrochlorination The other outlet of the reactor feed preheater is connected to the inlet of the desorption tower, the bottom outlet of the desorption tower is connected to the inlet of the reboiler of the desorption tower, and the outlet of the reboiler of the desorption tower is connected to the other inlet of the desorption tower. The outlet at the top of the tower is connected to the inlet of the total condenser of the desorption tower, the outlet of the total condenser of the desorption tower is connected to the inlet of the reflux tank of the desorption tower and the inlet of the tail cooler of the desorption tower, and the outlet of the tail cooler of the desorption tower is connected to the inlet of the reflux tank of the desorption tower The outlet of the desorption reflux tank is connected to the inlet of the liquid tank of the desorption tank, the outlet of the liquid tank of the desorption tank is connected to the inlet of the low boiling column, and the outlet of the lower part of the low boiling column is connected to the inlet of the reboiler of the low boiling column and the trichloro The inlet of the ethylene column is connected, the outlet of the reboiler of the low boiling column is connected with the other inlet of the low boiling column, the outlet of the top of the low boiling column is connected with the inlet of the total condenser of the low boiling column, and the outlet of the total condenser of the low boiling column is respectively It is connected with the inlet of the reflux tank of the low boiling tower and the inlet of the tail cooler of the low boiling tower. The outlet of the tail cooler of the low boiling tower is connected with the inlet of the reflux tank of the low boiling tower. The inlet of the trichlorethylene tank is connected to the inlet of the trichlorethylene tank, the outlet of the reboiler of the trichlorethylene tower is connected to the other inlet of the trichlorethylene tower, and the outlet of the upper part of the trichlorethylene tower is connected to the inlet of the total condenser of the trichlorethylene tower The ends are connected, and the outlet end of the total condenser of the trichlorethylene tower is divided Don't connect with the inlet end of the tail cooler of the trichlorethylene tower and the inlet end of the reflux tank of the trichlorethylene tower, the outlet end of the tail cooler of the trichlorethylene tower is connected with the inlet end of the reflux tank of the trichlorethylene tower, and the outlet end of the reflux tank of the trichlorethylene tower is respectively connected with the The other inlet end of the ethylene tower is connected to the inlet end of the trichlorethylene discharge cooler, the outlet end of the trichlorethylene kettle liquid tank is connected to the inlet end of the middle distillate column, and the outlet end of the lower part of the middle distillate tower is respectively connected to the inlet end of the reboiler of the middle distillate column It is connected with the inlet of the tetrachlorethylene tower, the upper outlet of the middle distillate tower is connected with the inlet of the total condenser of the middle distillate tower, and the outlet of the total condenser of the middle distillate tower is respectively connected with the inlet of the tail cooler of the middle distillate tower and the inlet of the reflux tank of the middle distillate tower The outlet end of the tail cooler of the middle distillate tower is connected with the other inlet end of the reflux tank of the middle distillate tower, the outlet end of the reflux tank of the middle distillate tower is connected with the other inlet end of the liquid tank of the desorption tower, and the outlet end of the lower part of the tetrachlorethylene tower is connected with the four The inlet end of the reboiler of the chloride tower, the outlet end of the upper part of the tetrachlorethylene tower are connected with the inlet end of the total condenser of the tetrachlorethylene tower, and the outlet end of the total condenser of the tetrachlorethylene tower is respectively connected with the inlet end of the reflux tank of the tetrachlorethylene tower and the inlet end of the tetrachlorethylene tower. The inlet end of the ethylene tail cooler is connected, the outlet end of the tetrachlorethylene tail cooler is connected with the other inlet end of the reflux tank of the tetrachlorethylene tower, and the heat exchange devices of each total condenser and each tail cooler are made of modified phenolic resin impregnated graphite pieces.

The trichlorethylene industrial production device adopting the above-mentioned structure has a reasonable structure, a large production capacity, and can operate safely and stably for a long period. The produced trichlorethylene products are of high quality.

Description of drawings

Fig. 1 is a schematic diagram of a part of the structure of the utility model.

Fig. 2 is a schematic diagram of another part of the structure of the utility model.

Fig. 3 is a schematic diagram of the structure of the acetylene gas drying and purifying device in the utility model.

Fig. 4 is the schematic diagram of the structure of the dehydrochlorination reaction device in the utility model.

Fig. 5 is a schematic diagram of the structure of the gas distributor in the utility model.

Fig. 6 is a sectional view along A-A of Fig. 5 .

Figure 7 shows the assembly relationship of the main and branch distribution pipes.

Fig. 8 is a B-B sectional view of Fig. 5 .

Detailed ways

Further illustrate the utility model below in conjunction with accompanying drawing.

As shown in the accompanying drawings, the trichlorethylene industrialized production device of the present utility model has an acetylene inlet pipeline and a chlorine gas inlet pipeline to be connected with the chlorination tower 9 inlets respectively, and the chlorination tower 9 outlets are fully condensed with the chlorination tower 7 inlets of the chlorination tower are connected to each other, and the 7 outlets of the chlorination tower total condenser are respectively connected to the chlorination reflux tank 8 inlets and the chlorination tower tail cooler 6 inlets, and the chlorination tower tail cooler 6 outlets are respectively connected to the chlorination reflux tank 8 The inlet end is connected to the inlet end of the gas-liquid separator 5, the outlet end of the gas-liquid separator 5 is connected to the inlet end of the exhaust buffer tank 4, the outlet end of the exhaust buffer tank 4 is connected to the inlet end of the hydraulic jet pump 3, and the outlet end of the hydraulic jet pump 3 is connected to the The inlet of the chlorinated tail water tank 10 is connected, the outlet of the chlorinated tail water tank 10 is connected to the inlet of the chlorinated tail water tank 1, the outlet of the chlorinated tail water tank 1 is connected to the inlet of the pressurized water pump 2, and the outlet of the pressurized water pump 2 is connected to the hydraulic Jet pump 3 is connected to the other inlet end, and the outlet end of chlorination reflux tank 8 is connected to the inlet end of crude tetrachloroethane tank 11, and the outlet end of crude tetrachloroethane tank 11 is connected to the inlet end of tetrachloroethane tower 12, and the tetrachloroethane The outlet end of the lower part of the ethane tower 12 is connected with the inlet end of the tetrachloroethane tower reboiler 13 and the inlet end of the refined tetrachloroethane tank 17 respectively, and the outlet end of the tetrachloroethane tower reboiler 13 is connected with the tetrachloroethane tower 12 The other inlet end of the tetrachloroethane tower is connected, the tetrachloroethane tower 12 top outlet ports are connected with the tetrachloroethane tower full condenser 14 inlet ports, and the tetrachloroethane tower full condenser 14 outlet ports are respectively connected with the tetrachloroethane tower reflux tank 16 inlet port is connected with tetrachloroethane tail cooler 15 inlet port, tetrachloroethane tail cooler 15 outlet port is connected with tetrachloroethane tower reflux tank 16 inlet port, refined tetrachloroethane tank (17) outlet port It is connected to the inlet of the tetrachloroethane vaporizer 18, the outlet of the tetrachloroethane vaporizer is connected to the inlet of the feed preheater 21 of the dehydrochlorination reactor, and the outlet of the feed preheater 21 of the dehydrochlorination reactor is preheated with the heat transfer oil The inlet of the device 19 is connected, the outlet of the heat transfer oil preheater 19 is connected with the inlet of the dehydrochlorination reaction device 20, the outlet of the dehydrochlorination reaction device 20 is connected with the other inlet of the feed preheater 21 of the dehydrochlorination reactor, and the dehydrochlorination The other outlet of the reactor feed preheater 21 is connected to the inlet of the desorption tower 22, the outlet of the bottom of the desorption tower 22 is connected to the inlet of the reboiler (23) of the desorption tower, and the outlet of the reboiler 23 of the desorption tower is connected to the inlet of the desorption tower 22 is connected to the other inlet port, the outlet port on the top of the desorption tower is connected to the inlet port of the total condenser 24 of the desorption tower, and the outlet port of the total condenser of the desorption tower is connected to the inlet port of the reflux tank 26 of the desorption tower and the inlet port of the tail cooler 25 of the desorption tower respectively. The outlet end of the tower tail cooler 25 is connected to the inlet end of the desorption tower reflux tank 26, the outlet end of the desorption reflux tank 26 is connected to the inlet end of the desorption tank liquid tank 27, and the outlet end of the desorption tank liquid tank 27 is connected to the inlet end of the low boiling tower 28, the low boiling tank The outlet end of the lower part of the tower 28 is connected with the inlet port of the low boiling tower reboiler 29 and the inlet port of the trichlorethylene tower 33 respectively, the outlet port of the reboiler of the low boiling tower is connected with the other inlet end of the low boiling tower, and the outlet port at the top of the low boiling tower 28 is end is connected with the inlet end of the low boiling column total condenser 30, and the outlet end of the low boiling column total condenser 30 is respectively connected with the inlet port of the low boiling column reflux tank 32 and the inlet end of the low boiling column tail cooler 31, The outlet of the tail cooler 31 of the low boiling tower is connected to the inlet of the reflux tank 32 of the low boiling tower, and the outlet of the lower part of the trichlorethylene tower 33 is respectively connected to the inlet of the reboiler 34 of the trichlorethylene tower and the inlet of the trichlorethylene kettle liquid tank 39 , the outlet end of the trichlorethylene tower reboiler 34 is connected with the other inlet end of the trichlorethylene tower 33, the outlet end of the upper part of the trichlorethylene tower 33 is connected with the inlet end of the trichlorethylene tower full condenser 35, and the trichlorethylene tower full condenser The outlet end of device 35 is connected with the inlet end of trichlorethylene tower tail cooler 36 and the inlet end of trichlorethylene tower reflux tank 37 respectively, the outlet end of trichlorethylene tower tail cooler 36 is connected with the inlet end of trichlorethylene reflux tank 37, and the trichlorethylene tower tail cooler 37 inlet end is connected. The outlet of the reflux tank 37 is connected to the other inlet of the trichlorethylene tower 33 and the inlet of the trichlorethylene discharge cooler 38, and the outlet of the trichlorethylene kettle liquid tank 39 is connected to the inlet of the middle distillate tower 40, and the middle distillate tower The outlet port of the lower part of the middle distillate column is connected with the inlet port of the reboiler 41 of the middle distillate column and the inlet port of the tetrachlorethylene column 45 respectively; The outlet end of 42 is respectively connected with the inlet end of middle distillate column tail cooler 43 and the inlet end of middle distillate column reflux tank 44, the outlet end of middle distillate column tail cooler 43 is connected with the other inlet end of middle distillate column reflux tank 44, and the middle distillate column reflux tank The 44 outlets are connected with the other inlet of the desorption tower kettle liquid tank 27, the outlet of the lower part of the tetrachlorethylene tower is connected with the inlet of the reboiler 46 of the tetrachlorethylene tower, and the outlet of the upper part of the tetrachlorethylene tower 45 is fully connected with the outlet of the tetrachlorethylene tower. Condenser 47 inlet end is connected, the outlet end of tetrachlorethylene tower total condenser 47 is connected with the inlet end of tetrachlorethylene tower reflux tank 49 and the inlet end of tetrachlorethylene tail cooler 48 respectively, the outlet end of tetrachlorethylene tail cooler 48 is connected with The other inlet end of the reflux tank 49 of the tetrachlorethylene tower is connected to each other, and the heat exchange devices of each total condenser and each tail cooler are graphite parts impregnated with modified phenolic resin. The structure of the heat exchange devices of each total condenser and each tail cooler is the same as that of the existing graphite material.

The specific work process of the production device of the present utility model is that the acetylene from the acetylene intake pipeline and the chlorine from the chlorine gas intake pipeline enter the chlorination tower 9, and after reacting in the mother liquor containing the catalyst, the gas phase enters the total condenser of the chlorination tower 7. Enter the chlorination tower reflux tank 8 after the initial condensation of the circulating water, the uncondensed gas phase enters the chlorination tower tail cooler 6, and the liquid phase after deep condensation of frozen brine flows into the chlorination tower reflux tank 8, and the non-condensable gas is vacuumed Pumped to the gas-liquid separator 5, the liquid phase separated by the gas-liquid separator 5 enters the crude tetrachloroethane tank 11, the gas phase enters the tail gas buffer tank 4, and the tail gas in the tail gas buffer tank enters the hydraulic jet pump 3, and the hydraulic jet pump is used Vacuuming according to the change of the flow rate, the water from the hydraulic jet pump directly enters the chlorination tail water tank 10, the water in the tail water tank flows into the tail water tank 1, and the water in the tail water tank is recycled after being treated. The crude tetrachloroethane from the crude tetrachloroethane tank 11 is transported to the tetrachloroethane tower 12, and after the tetrachloroethane tower reboiler 13 is heated and rectified and separated, the rising gas phase in the tower passes through the tetrachloroethane tower The total condenser 14 exchanges heat with circulating water, the condensate flows into the tetrachloroethane reflux tank 16, the uncondensed gas phase enters the tetrachloroethane tail cooler 15 and exchanges heat with frozen brine, and the liquid phase flows into the tetrachloroethane reflux tank 16 , The non-condensable gas is vented under the protection of nitrogen, most of the materials in the tetrachloroethane reflux tank are refluxed, and a small amount is extracted to the finished product tank. The tetrachloroethane from the refined tetrachloroethane tank 17 is sent to the tetrachloroethane vaporizer 18, and the vaporized gas enters the dehydrochlorination reactor feed preheater 21 and performs heat exchange with the gas coming out of the dehydrochlorination reaction device 20 , then to the heat conduction oil preheater 19, enter the dehydrochlorination reaction device 20 after being heated to the required temperature by the heat conduction oil, and the mixed gas after the reaction of the dehydrochlorination reactor enters after the dehydrochlorination reactor feed preheater 21 cools down Desorption tower 22, the condensable gas in the rising gas phase in the tower is cooled by the desorption tower total condenser 24 with circulating water, the liquid phase enters the desorption tower reflux tank 26, and the uncondensed gas phase enters the desorption tower tail cooler 25, and after being deeply condensed by frozen brine The liquid phase flows into the desorption reflux tank 26, and the non-condensable gas can be sent to the hydrogen chloride absorption section. The materials in the desorption tower reflux tank are all refluxed to the desorption tower 22, and the desorption tower reboiler 23 connected to the desorption tower heats the materials to make the tower There is a large amount of rising material vapor in it, so that the acidity of the desorption tower still liquid is qualified, and the desorption tower still material enters the desorption tower still liquid tank 27, and the material in the desorption still liquid tank is sent to the low boiling tower 28, and passes through the low boiling tower reboiler 29 heating, after rectification and separation, the rising gas phase in the tower is condensed by the low-boiling tower total condenser 30, the liquid phase enters the low-boiling tower reflux tank 32, and the uncondensed gas enters the low-boiling tower tail cooler 31 and after exchanging heat with frozen brine, The liquid phase flows into the reflux tank 32 of the low boiling column, and the non-condensable gas is vented under the protection of nitrogen. Most of the materials in the reflux tank of the low boiling column are refluxed, and a small amount is extracted to the finished product tank. The materials in the low-boiling tower are transported to the trichlorethylene tower 33, heated by the trichlorethylene tower reboiler 34, and rectified and separated. The trichlorethylene tower reflux tank 37, the uncondensed gas enters the trichlorethylene tower tail cooler 36, and after being condensed by frozen brine, the liquid phase enters the trichlorethylene tower reflux tank 37, the uncondensed gas is vented under the protection of nitrogen, and the trichlorethylene tower refluxes The condensate in the tank is refluxed to the top of the tower, and the material at the top of the tower is extracted to the finished product tank through the side line, and the liquid in the tower still is transported to the liquid tank 39 of the trichlorethylene tower. The material in the liquid tank 39 of the trichlorethylene tower is transported to the middle distillate tower 40. After the material enters the middle distillate tower, it is heated by the reboiler 41 of the middle distillate tower. After heat exchange between the device 42 and the circulating water, the condensed liquid enters the middle distillate column reflux tank 44, and the non-condensed gas phase enters the middle distillate column tail cooler 43 and after exchanging heat with frozen brine, the liquid phase flows into the middle distillate column reflux tank 44, and the non-condensable gas phase enters the middle distillate column reflux tank 44. Empty under the protection of nitrogen, part of the condensate in the reflux tank of the middle distillate column is refluxed to the top of the middle distillate column through the pipeline, and the other part is extracted to the liquid tank 27 of the desorption column. The liquid in the middle distillate tower is transported to the tetrachlorethylene tower 45, and the material in the tetrachlorethylene tower 45 is heated by the tetrachlorethylene tower reboiler. After rectification and separation, the rising steam in the tower passes through the tetrachlorethylene tower total condenser 47 and After the circulating water heat exchange, the condensate enters the tetrachlorethylene tower reflux tank 49, and the non-condensable gas phase enters the tetrachlorethylene tower tail cooler 48 and after heat exchange with the circulating water, the liquid phase flows into the tetrachlorethylene tower reflux tank 49, and the non-condensable gas phase enters the tetrachlorethylene tower reflux tank 49. Vent under the protection of nitrogen, part of the condensate in the reflux tank of the tetrachlorethylene tower is refluxed to the top of the tetrachlorethylene tower through the pipeline, and the other part is extracted to the tetrachlorethylene metering tank, and the liquid in the bottom of the tower is transported to the raffinate tank.

Each inlet port and outlet port are connected through pipelines respectively.

The working principles of pressurized water pumps, hydraulic jet pumps, chlorination towers, rectification towers, vaporizers, dehydrochlorination reactors, heat exchangers and other equipment are the same as those of existing corresponding equipment.

Tetrachloroethane reflux tank 16 outlet is connected with finished product tank inlet.

The outlet end of the triene discharge cooler 38 is connected with the trichlorethylene metering tank.

The outlet end of the lower part of the tetrachlorethylene tower 45 is also connected with the inlet end of the raffinate tank.

The outlet end of the reflux tank 49 of the tetrachlorethylene tower is respectively connected with the inlet end of the tetrachlorethylene tower 45 and the inlet end of the tetrachlorethylene metering tank through pipelines.

As shown in Figure 3, the acetylene inlet pipeline is connected to the inlet of the chlorination tower 9 through the acetylene gas drying and purification device 50, and the acetylene gas inlet pipeline 523 and the acetylene compressor 51 inlet are arranged on the acetylene gas drying and purification device 50 The outlet of acetylene compressor 51 is connected to the inlet of acetylene cooler 52, the outlet of acetylene cooler is connected to the inlet of acetylene mist catcher 53, the upper outlet of acetylene mist catcher is connected to the lower inlet of sulfuric acid drying tower 56, The upper outlet of sulfuric acid drying tower I is connected to the lower inlet of sulfuric acid drying II tower 59, the upper outlet of sulfuric acid drying II tower is connected to the lower inlet of sulfuric acid drying III tower 512, and the upper outlet of sulfuric acid drying III tower is connected to the inlet of acetylene deacidifier 515 The upper outlet of the acetylene deacidifier is connected to the inlet of the acetylene adsorption tower 517, the other outlet of the acetylene cooler 52 is connected to the inlet of the moisture collection tank 54, and the lower outlet of the acetylene mist catcher 53 is connected to the inlet of the moisture collection tank 54 The outlet of the concentrated sulfuric acid storage tank 520 is connected to the inlet of the concentrated sulfuric acid delivery pump 522, the outlet of the concentrated sulfuric acid delivery pump is connected to the inlet of the concentrated sulfuric acid cooler 514, and the outlet of the concentrated sulfuric acid cooler is connected to the upper inlet of the sulfuric acid drying III tower 512 The ends are connected, the outlet end of the lower part of the sulfuric acid drying tower 512 is connected with the lower inlet port of the sulfuric acid drying tower 59, the other lower outlet port of the sulfuric acid drying tower 512 is connected with the inlet port of the sulfuric acid circulating pump 513 of the sulfuric acid drying tower III, and the sulfuric acid drying tower III The outlet of circulating pump 513 is connected to the inlet of dilute sulfuric acid circulating cooler 511, the outlet of dilute sulfuric acid circulating cooler 511 is connected to the upper inlet of sulfuric acid drying tower III 512, the outlet of the lower part of sulfuric acid drying II tower 59 is connected to the lower part of sulfuric acid drying tower I 56 The inlet end is connected, the outlet end of the other lower part of the sulfuric acid drying tower II is connected with the inlet end of the sulfuric acid circulation pump 510 of the sulfuric acid drying II tower, the outlet end of the sulfuric acid circulation pump 510 of the sulfuric acid drying tower II is connected with the inlet end of another dilute sulfuric acid circulating cooler 58, The outlet of another dilute sulfuric acid circulating cooler 58 is connected to the upper inlet of the sulfuric acid drying tower II tower 59, the outlet of the lower part of the sulfuric acid drying tower I tower 56 is connected to the inlet port of the sulfuric acid circulating pump 57 of the sulfuric acid drying tower I, and the sulfuric acid circulating pump 57 of the sulfuric acid drying tower I The outlet end is connected to the inlet end of the third dilute sulfuric acid circulating cooler 55, the outlet end of the third dilute sulfuric acid circulating cooler 55 is connected to the upper inlet end of the sulfuric acid drying tower 56, and the other lower outlet port of the sulfuric acid drying tower 56 is connected to the dilute sulfuric acid storage The tank 519 is connected, and the nitrogen buffer tank 521 is connected with the lower inlet port of the acetylene adsorption tower 517 through the nitrogen electric heater 518 .

The specific working process of the drying and purification device is that the acetylene gas enters the acetylene compressor 51 and is compressed until the gas pressure rises to 0.135~0.15Mpa, and then enters the acetylene cooler 52 to cool down to 2~5°C, and the cooled acetylene gas passes through the acetylene to catch mist After the device 53 collects the mist, it enters the sulfuric acid drying tower 56 to dry with about 88% sulfuric acid, then enters the sulfuric acid drying tower 59 to dry with about 92% sulfuric acid, and then enters the sulfuric acid drying tower 512 to use 98% concentrated sulfuric acid Further drying. Finally, the acetylene gas is collected by the acetylene acid remover 515 to capture the acid mist, and then enters the acetylene adsorption tower for further purification. The water content of the treated acetylene gas is 60-70ppm. Due to the strong oxidation of concentrated sulfuric acid, the acetylene is also removed. Other impurities in the gas play a dual role in removing water and purifying the acetylene gas. The traditional method of drying and purifying acetylene gas adopts the freezing method, that is, cooling the acetylene to about 0°C with cold brine. The water content of acetylene gas can only be reduced to 200-300ppm, and if the temperature is too low, the pipeline will freeze, threatening normal production.

When driving for the first time, the water in the acetylene mist catcher 53 and the moisture collection tank 54 is added by the tap water line. During the normal production process, the condensed water condensed by the acetylene cooler 52 and the acetylene mist catcher 53 flows to the moisture collection tank 54 respectively, and then is regularly discharged to the sewer.

塔59中的硫酸超过一定液位时溢流入硫酸干燥Ⅰ塔56，硫酸干燥塔59底部的硫酸由硫酸干燥Ⅱ塔硫酸循环泵510输送至另一稀硫酸循环冷却器58冷却后，进入硫酸干燥塔59，形成酸循环。硫酸干燥Ⅰ塔56底部的硫酸由硫酸干燥Ⅰ塔硫酸循环泵57输送至第三稀硫酸循环冷却器55冷却后，进入硫酸干燥Ⅰ塔56，形成酸循环。硫酸干燥Ⅰ塔56底部的硫酸液位达到一定液位值时排至稀硫酸储罐519。乙炔除酸器515捕集的酸雾自流至硫酸收集罐516，然后再排放至稀硫酸储罐519。初次开车时，各硫酸干燥塔和乙炔除酸器515中的硫酸，都要由浓硫酸输送泵522先注入至规定液位。The specific working process of sulfuric acid drying is: the concentrated sulfuric acid with a purity of 98% from the concentrated sulfuric acid storage tank 520 is transported by the concentrated sulfuric acid delivery pump 522 to the concentrated sulfuric acid cooler 514 and cooled, then sent to the sulfuric acid drying tower 512, and dried in sulfuric acid When the sulfuric acid in the III tower 512 exceeds a certain level, it overflows into the sulfuric acid drying tower II 59, and the sulfuric acid at the bottom of the sulfuric acid drying III tower 512 is transported to the dilute sulfuric acid circulating cooler 511 by the sulfuric acid circulating pump 513 of the sulfuric acid drying III tower, and then enters the sulfuric acid drying III Tower 512, forming an acid cycle. drying in sulfuric acid

When the sulfuric acid in the tower 59 exceeds a certain level, it overflows into the sulfuric acid drying tower 56, and the sulfuric acid is dried The sulfuric acid at the bottom of the tower 59 is transported by the sulfuric acid circulating pump 510 of the sulfuric acid drying II tower to another dilute sulfuric acid circulating cooler 58 for cooling, and then enters the sulfuric acid drying Tower 59, forming an acid cycle. The sulfuric acid at the bottom of the sulfuric acid drying tower 56 is transported by the sulfuric acid drying tower I sulfuric acid circulation pump 57 to the third dilute sulfuric acid circulating cooler 55 for cooling, and then enters the sulfuric acid drying tower 56 to form an acid cycle. When the sulfuric acid liquid level at the bottom of the sulfuric acid drying tower 56 reaches a certain level, it is discharged to the dilute sulfuric acid storage tank 519. The acid mist collected by the acetylene acid remover 515 flows to the sulfuric acid collection tank 516 by itself, and then is discharged to the dilute sulfuric acid storage tank 519 . When driving for the first time, the sulfuric acid in each sulfuric acid drying tower and acetylene acid remover 515 must be injected to the specified liquid level by the concentrated sulfuric acid delivery pump 522.

The nitrogen gas enters the nitrogen buffer tank 521 through the nitrogen gas inlet pipeline, and enters the acetylene adsorption tower 517 after being heated by the nitrogen electric heater 518 . Each inlet port and outlet port are connected through pipelines respectively. The structures and working principles of acetylene compressors, acetylene coolers, acetylene mist traps, sulfuric acid drying towers, acetylene deacidifiers, acetylene adsorption towers, sulfuric acid coolers, and nitrogen electric heaters 518 are the same as those of existing corresponding equipment . In order to improve the cooling effect, a two-stage acetylene cooler can be used, the outlet of the primary acetylene cooler is connected to the inlet of the secondary acetylene cooler, and the outlet of the secondary acetylene cooler is connected to the inlet of the acetylene mist catcher 53 . The acetylene adsorption tower adopts molecular sieve adsorption tower.

As shown in Figure 4, on the described dehydrochlorination reaction device 20, there are at least 3 tetrachloroethane vaporizers 202, also have the dehydrochlorination reactor 206 identical with tetrachloroethane vaporizer, each tetrachloroethane The inlets of the vaporizers are respectively connected to each other with the feed pipeline 201 through valves, the outlets of each tetrachloroethane vaporizers are respectively connected with the inlets of the dehydrochlorination reactors through valves, and the outlets of each dehydrochlorination reactors are respectively connected with the discharge pipeline 209 through valves, The outlets of each dehydrochlorination reactor are also connected through valves and pipelines 208, the inlets of each dehydrochlorination reactors are also connected through valves and another pipeline 205, and the pipelines and another pipeline are connected by connecting pipelines 207, each The outlet of the tetrachloroethane vaporizer is also connected through a valve and a third pipeline 203 .

In this dehydrochlorination reaction device, each tetrachloroethane vaporizer is connected in series with a dehydrochlorination reactor to form a group of reaction systems. At the same time, through the connection control of pipelines and valves, the inlet pipeline of each dehydrochlorination reactor is The outlet pipeline and the outlet pipeline of the tetrachloroethane vaporizer are respectively connected to each other. In this way, each tetrachloroethane vaporizer can be operated in series with any dehydrochlorination reactor, and any two dehydrochlorination reactors can be operated in series. During normal production, two sets of reaction systems are operated, and one set of reaction systems is used for standby, that is, two sets of reaction systems are used for backup. When the dehydrochlorination reaction catalyst activity of a certain group of reaction systems drops below 50%, the operation of this group of reaction systems is stopped, and the third group of reaction systems is started. In order to further utilize the activity of the catalyst in the dehydrochlorination reaction system of parking, reduce the unit consumption of trichlorethylene, the dehydrochlorination reactor outlet in the third group of reaction system is connected in series with the dehydrochlorination reactor inlet of parking (that is, restart the catalyst dehydrochlorination reactor with reduced activity) operates. In this way, the activity of the dehydrochlorination catalyst can be fully utilized, which can ensure a high yield of the dehydrochlorination reaction and avoid waste of the catalyst. The outlets of the tetrachloroethane vaporizers are also connected to each other through valves and fourth pipelines 204 . Through the dehydrochlorination reaction device of above-mentioned structure, and tetrachloroethane tower, desorption tower, low boiling tower, trichlorethylene tower, middle distillate tower and the enlargement of production capacity of tetrachlorethylene tower, can make trichloride of the present utility model The ethylene industrial production plant has a production capacity of 40,000 tons/year of trichlorethylene.

As shown in Figures 5-8, on the gas distributor in the chlorination tower 9, there is a main distribution pipe 91, the two ends of the main distribution pipe are connected horizontally with short branch distribution pipes 92, and the middle part is horizontally connected with long branch pipes. Distributing pipe 94, between the short-branch distribution pipe and the long-branch distribution pipe, there is a middle-branch distribution pipe 93 horizontally connected to the main distribution pipe, and there is a vent hole in the vertical direction and on both sides of the vertical direction of the lower half circumference of the main distribution pipe wall 101. Multiple rows of air outlet holes 301 are distributed on the lower half circumference of the pipe wall of each branch distribution pipe.

During use, after the gas distributor is packed in the chlorination tower, a blocking plate 95 is installed at both ends of each branch distribution pipe, and is fixed on the fittings on the inner wall of the acetylene chlorination tower by U-shaped bolts 910 . Another blocking plate 96 is installed at the end of the main distribution pipe, and is fixed on the mounting piece of the inner wall of the acetylene chlorination tower by another U-bolt 911 . Each branch distribution pipe can pass through the main distribution pipe, and the through hole 302 on the branch distribution pipe communicates with the inner cavity of the main distribution pipe. The bolts 97 passing through the main and branch distribution pipes and the nuts 98 at both ends of the bolts fix the main and branch distribution pipes together. Gas enters from the port 99 exposed outside the acetylene chlorination tower of the main distribution pipe, and is distributed in the acetylene chlorination tower through the air outlet holes on each pipe. The gas distributor with this structure improves the distribution effect of chlorine gas and acetylene in the chlorination mother liquor, significantly enhances the gas distribution effect, improves the yield of chlorination reaction, and maintains the purity of crude tetrachloroethane at 97- 98%, 3-4% higher than the same industry in China. The phenomenon of explosion caused by contact of acetylene gas and chlorine gas due to uneven distribution and incomplete reaction is prevented.

The shell side of the total condenser of the trichlorethylene tower, the shell side of the trichlorethylene discharge cooler, the trichlorethylene metering tank, and the trichlorethylene storage tank are replaced by stainless steel from carbon steel, which effectively ensures that the trichlorethylene product has a better quality The chromaticity avoids the pollution of the product due to the corrosion of the carbon steel material.

The rectification section of the tetrachloroethane tower and the rectification section of the desorption tower are made of enamel, and the rectification section of the low boiling tower is made of polyvinyl fluoride (F40) column section. In order to improve the rectification effect of the trichlorethylene tower, the tower is designed as a valve tower. In order to improve the service life of the tray, the material of the float valve and the tray is designed to be stainless steel. In this way, the corrosion resistance and rectification effect of the rectification section of each tower are greatly improved.

In the presence of oxygen, trichlorethylene and other intermediate products can react to produce organic acids, resulting in product deterioration and increased consumption. In order to avoid contact of trichlorethylene and other intermediate products with oxygen, nitrogen sealing devices are designed and used on the metering tanks and storage tanks in the intermediate tank area and finished product tank area, so that the excess space in the container is occupied by nitrogen. The quality of the product is guaranteed and the decomposition of trichlorethylene is avoided.

The raw materials for the production of trichlorethylene are chlorine gas and acetylene. Chlorine gas is a highly toxic medium, and acetylene is chemically active, flammable and explosive. In order to further improve the safety of production, the device of the utility model is provided with multiple interlocks, which are the interlocks between the inlet and outlet pressure of the acetylene compressor and the compressor, the interlock between the compressor and the chlorine gas and acetylene regulating valve, and the tail The interlocking between the water flow and the chlorine and acetylene regulating valves, the interlocking between the vacuum degree of the chlorination tower and the chlorine and acetylene regulating valves, etc., ensure the safe and stable operation of the trichlorethylene plant through the above interlocking.

The chlorination tower operates under negative pressure, and the negative pressure is generated by suction with a hydraulic jet pump. During the pumping process, part of hydrogen chloride gas, acetylene gas, chlorine gas and organic acids are dissolved in the tail water, which gradually increases the acidity of the tail water. Other trichlorethylene manufacturers replace the tail water when the acidity of the tail water reaches a certain value, which not only pollutes the environment but also wastes water resources. The device of the utility model transports the tail water in the tail water tank to the hydraulic jet pump with the tail water pressurized pump, sucks the chlorination tower to generate negative pressure, and the tail water overflows to the tail water tank through the chlorination tail water tank , recycling, saving a lot of water resources and protecting the environment.

The trichlorethylene towers of other trichlorethylene manufacturers use the top reflux liquid to discharge, and the acid content of the product is 10-15ppm or higher. When trichlorethylene is used as a metal cleaning agent, it can corrode the metal surface and damage the cleaned product. Objects, causing serious losses to manufacturers who use trichlorethylene as a cleaning agent. On the device of the present utility model, four side outlets are added to the trichlorethylene tower, which are respectively arranged on the 5th, 7th, 9th, and 11th floor trays of the rectifying section. The combination of tower top discharge and upper side discharge can effectively reduce the acidity of trichlorethylene products, and the acidity can be controlled below 5ppm.

Claims (4)

1. trieline industrial production device, it is characterized in that, it has the acetylene admission line to link to each other with chlorination tower (9) entrance end respectively with the chlorine admission line, chlorination tower (9) exit end links to each other with chlorination tower complete condenser (7) entrance end, chlorination tower complete condenser (7) exit end links to each other with chlorination return tank (8) entrance end and chlorination tower tail cooler (6) entrance end respectively, chlorination tower tail cooler (6) exit end links to each other with chlorination return tank (8) entrance end and gas-liquid separator (5) entrance end respectively, gas-liquid separator (5) exit end links to each other with tail gas buffer (4) entrance end, tail gas buffer (4) exit end links to each other with hydraulic jet pump (3) entrance end, hydraulic jet pump (3) exit end links to each other with chlorination tail tank (10) entrance end, chlorination tail tank (10) exit end links to each other with chlorination afterbay (1) entrance end, chlorination afterbay (1) exit end links to each other with pressure pump (2) entrance end, pressure pump (2) exit end links to each other with another entrance end of hydraulic jet pump (3), chlorination return tank (8) exit end links to each other with thick tetrachloroethane jar (11) entrance end, thick tetrachloroethane jar (11) exit end links to each other with tetrachloroethane tower (12) entrance end, tetrachloroethane tower (12) lower part outlet end links to each other with tetrachloroethane tower reboiler (13) entrance end and smart tetrachloroethane jar (17) entrance end respectively, tetrachloroethane tower reboiler (13) exit end links to each other with another entrance end of tetrachloroethane tower (12), tetrachloroethane tower (12) top exit end links to each other with tetrachloroethane tower complete condenser (14) entrance end, tetrachloroethane tower complete condenser (14) exit end links to each other with tetrachloroethane tower return tank (16) entrance end and tetrachloroethane tower tail cooler (15) entrance end respectively, tetrachloroethane tail cooler (15) exit end links to each other with tetrachloroethane tower return tank (16) entrance end, smart tetrachloroethane jar (17) exit end links to each other with tetrachloroethane vaporizer (18) entrance end, tetrachloroethane vaporizer exit end links to each other with dehydrochlorination reaction device feed preheater (21) entrance end, dehydrochlorination reaction device feed preheater (21) exit end links to each other with thermal oil preheater (19) entrance end, thermal oil preheater (19) exit end links to each other with dehydrochlorination reaction device (20) entrance end, dehydrochlorination reaction device (20) exit end links to each other with another entrance end of dehydrochlorination reaction device feed preheater (21), another exit end of dehydrochlorination reaction device feed preheater (21) links to each other with desorption tower (22) entrance end, desorption tower (22) outlet at bottom end links to each other with desorption tower reboiler (23) entrance end, desorption tower reboiler (23) exit end links to each other with another entrance end of desorption tower (22), desorption tower top exit end links to each other with desorption tower complete condenser (24) entrance end, desorption tower complete condenser exit end links to each other with desorption tower return tank (26) entrance end and Analytic Tower tail cooler (25) entrance end respectively, Analytic Tower tail cooler (25) exit end links to each other with desorption tower return tank (26) entrance end, desorb return tank (26) exit end links to each other with extraction-container flow container (27) entrance end, extraction-container flow container (27) exit end links to each other with low tower (28) entrance end that boils, low tower (28) the lower part outlet end that boils links to each other with low tower reboiler (29) entrance end and trieline tower (33) entrance end of boiling respectively, the low tower reboiler exit end that boils links to each other with low another entrance end of tower that boils, low tower (28) the top exit end that boils links to each other with low tower complete condenser (30) entrance end that boils, low tower complete condenser (30) exit end that boils reaches low tower tail cooler (31) entrance end that boils with low tower return tank (32) entrance end that boils respectively and links to each other, low tower tail cooler (31) exit end that boils links to each other with low tower return tank (32) entrance end that boils, trieline tower (33) lower part outlet end links to each other with trieline tower reboiler (34) entrance end and trieline still flow container (39) entrance end respectively, trieline tower reboiler (34) exit end links to each other with another entrance end of trieline tower (33), trieline tower (33) top exit end links to each other with trieline tower complete condenser (35) entrance end, trieline tower complete condenser (35) exit end links to each other with trieline tower tail cooler (36) entrance end and trieline tower return tank (37) entrance end respectively, trieline tower tail cooler (36) exit end links to each other with trieline return tank (37) entrance end, trieline return tank (37) exit end respectively with another entrance end of trieline tower (33), trieline discharging water cooler (38) entrance end links to each other, trieline still flow container (39) exit end links to each other with middle runnings tower (40) entrance end, middle runnings tower (40) lower part outlet end links to each other with middle runnings tower reboiler (41) entrance end and zellon tower (45) entrance end respectively, middle runnings tower (40) top exit end links to each other with middle runnings tower complete condenser (42) entrance end, middle runnings tower complete condenser (42) exit end links to each other with middle runnings tower tail cooler (43) entrance end and middle runnings tower return tank (44) entrance end respectively, middle runnings tower tail cooler (43) exit end links to each other with another entrance end of middle runnings tower return tank (44), middle runnings tower return tank (44) exit end links to each other with another entrance end of desorption tower still flow container (27), zellon tower (45) lower part outlet end and zellon tower reboiler (46) entrance end, zellon tower (45) top exit end links to each other with zellon tower complete condenser (47) entrance end, zellon tower complete condenser (47) exit end links to each other with zellon tower return tank (49) entrance end and zellon tail cooler (48) entrance end respectively, zellon tail cooler (48) exit end links to each other described each complete condenser with another entrance end of zellon tower return tank (49), the heat exchange device of each tail cooler adopts the graphite piece of modified phenolic resin impregnate with tallow.

2. trieline industrial production device as claimed in claim 1, it is characterized in that, described acetylene admission line links to each other with chlorination tower (9) entrance end through acetylene gas dry decontamination device (50), on acetylene gas dry decontamination device (50), there is acetylene admission line (523) to link to each other with acetylene compressor (51) entrance end, acetylene compressor (51) exit end links to each other with acetylene water cooler (52) entrance end, acetylene cooler outlet end links to each other with acetylene spray catcher (53) entrance end, acetylene spray catcher top exit end links to each other with dry I tower (56) the lower inlet end of sulfuric acid, the dry I tower of sulfuric acid top exit end links to each other with dry II tower (59) the lower inlet end of sulfuric acid, the dry II tower of sulfuric acid top exit end links to each other with dry III tower (512) the lower inlet end of sulfuric acid, the dry III tower of sulfuric acid top exit end links to each other with acetylene acid separator (515) entrance end, acetylene acid separator top exit end links to each other with acetylene adsorption tower (517) entrance end, another exit end of acetylene water cooler (52) links to each other with moisture holding tank (54) entrance end, acetylene spray catcher (53) lower part outlet end links to each other with moisture holding tank (54) entrance end, vitriol oil storage tank (520) exit end links to each other with vitriol oil transferpump (522) entrance end, vitriol oil transferpump exit end links to each other with concentrated sulfuric acid cooler (514) entrance end, the concentrated sulfuric acid cooler exit end links to each other with dry III tower (512) the upper inlet end of sulfuric acid, dry III tower (512) the lower part outlet end of sulfuric acid links to each other with dry II tower (59) the lower inlet end of sulfuric acid, dry another lower part outlet end of III tower (512) of sulfuric acid links to each other with dry III tower sulfuric acid recycle pump (513) entrance end of sulfuric acid, dry III tower sulfuric acid recycle pump (513) exit end of sulfuric acid links to each other with dilute sulphuric acid recirculation cooler (511) entrance end, dilute sulphuric acid recirculation cooler (511) exit end links to each other with dry III tower (512) the upper inlet end of sulfuric acid, dry II tower (59) the lower part outlet end of sulfuric acid links to each other with dry I tower (56) the lower inlet end of sulfuric acid, dry another lower part outlet end of II tower (59) of sulfuric acid links to each other with dry II tower sulfuric acid recycle pump (510) entrance end of sulfuric acid, dry II tower sulfuric acid recycle pump (510) exit end of sulfuric acid links to each other with another dilute sulphuric acid recirculation cooler (58) entrance end, another dilute sulphuric acid recirculation cooler (58) exit end links to each other with dry II tower (59) the upper inlet end of sulfuric acid, dry I tower (56) the lower part outlet end of sulfuric acid links to each other with dry I tower sulfuric acid recycle pump (57) entrance end of sulfuric acid, dry I tower sulfuric acid recycle pump (57) exit end of sulfuric acid links to each other with the 3rd dilute sulphuric acid recirculation cooler (55) entrance end, the 3rd dilute sulphuric acid recirculation cooler (55) exit end links to each other with dry I tower (56) the upper inlet end of sulfuric acid, dry another lower part outlet end of I tower (56) of sulfuric acid links to each other with dilute sulphuric acid storage tank (519), and nitrogen buffer tank (521) links to each other with acetylene adsorption tower (517) lower inlet end through nitrogen electric heater (518).

3. trieline industrial production device as claimed in claim 1 or 2, it is characterized in that, on described dehydrochlorination reaction device (20), at least 3 tetrachloroethane vaporizers (202) are arranged, also have the quantity dehydrochlorination reaction device (206) identical with the tetrachloroethane vaporizer, the import of each tetrachloroethane vaporizer links to each other with feeding line (201) through valve respectively, the outlet of each tetrachloroethane vaporizer links to each other through the import of valve with the dehydrochlorination reaction device respectively, the outlet of each dehydrochlorination reaction device links to each other with discharging pipeline (209) through valve respectively, between the outlet of each dehydrochlorination reaction device also through valve, pipeline (208) links to each other, between the import of each dehydrochlorination reaction device also through valve, another pipeline (205) links to each other, pipeline, link to each other by connection line (207) between another pipeline, the outlet of each tetrachloroethane vaporizer is also through valve, the 3rd pipeline (203) links to each other.

4. as claim 1 or 2 or 3 described trieline industrial production devices, it is characterized in that, on the gas distributor in described chlorination tower (9), main distribution pipe (91) is arranged, main distribution pipe two ends are horizontally connected with a short distribution pipe (92), the middle part is horizontally connected with the distribution pipe of drawing money on credit (94), a short distribution pipe, draw money on credit have between the distribution pipe in distribution pipe (93) cross connection on main distribution pipe, vertical direction at main second circumference of distribution pipe tube wall, the vertical direction both sides have one to discharge pore (101) respectively, are distributed with many row's distribution pipe production wells (301) on second circumference of each distribution pipe tube wall.

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