CN215627707U - Realize resource recovery's crude chloroethylene clean system - Google Patents
Realize resource recovery's crude chloroethylene clean system Download PDFInfo
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- CN215627707U CN215627707U CN202121142514.2U CN202121142514U CN215627707U CN 215627707 U CN215627707 U CN 215627707U CN 202121142514 U CN202121142514 U CN 202121142514U CN 215627707 U CN215627707 U CN 215627707U
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Abstract
The utility model discloses a crude chloroethylene purification system for realizing resource recovery, which is characterized by comprising an acetylene pipeline, a hydrogen chloride pipeline, a mixer, a converter, a falling film absorber, a water washing tower, an industrial water pipeline, an alkaline washing tower, a dilute hydrochloric acid tank, a dilute hydrochloric acid cooler, a hydrochloric acid storage tank, a calcium chloride solution pipeline, a concentration tower, a jet mixer, a desorption tower, a hydrogen chloride cooler, a steam condenser and a waste water tank. The utility model has the advantages that: the utility model has simple connecting structure and easy realization; the recycling of hydrogen chloride resources is realized, the production cost of enterprises is reduced, and the economic benefit of the enterprises is improved; the recycling of water resources is realized, and the water consumption cost of enterprises is reduced; ensuring the normal operation of the system; the utility model realizes the automatic configuration of the washing alkali liquor of the alkaline washing tower, saves the labor cost and saves time and labor.
Description
The technical field is as follows:
the utility model relates to a purification system, in particular to a crude chloroethylene purification system for realizing resource recovery.
Background art:
the most common economic and feasible method is that hydrogen chloride gas is slightly excessive, and most of excessive hydrogen chloride is removed from the reacted crude vinyl chloride gas through a falling film absorber and a water washing tower of a crude vinyl chloride purification system to generate concentrated hydrochloric acid with the mass fraction of about 31 percent, but the obtained concentrated hydrochloric acid carries trace mercury, iron and other impurities in the reaction process, has low quality, can only be applied to occasions with low requirements and has low economic benefit; after passing through the water washing tower, performing alkali washing through an alkali washing tower to further remove hydrogen chloride and carbon dioxide, completing purification of the crude chloroethylene, and sending the purified crude chloroethylene gas to a rectification system for rectification to obtain refined chloroethylene; when the purification system operates at low load, the pressure of the system is unstable, and the normal operation of production is affected.
The utility model has the following contents:
the utility model aims to provide a crude chloroethylene purification system which is simple in connection structure, realizes the recycling of hydrogen chloride resources and realizes the recycling of waste water and the resource recycling.
The utility model is implemented by the following technical scheme: the purpose of the patent provides a crude chloroethylene purification system for realizing resource recovery, which is characterized by comprising an acetylene pipeline, a hydrogen chloride pipeline, a mixer, a converter, a falling film absorber, a water scrubber, an industrial water pipeline, an alkaline washing tower, a dilute hydrochloric acid tank, a dilute hydrochloric acid cooler, a hydrochloric acid storage tank, a calcium chloride solution pipeline, a concentration tower, a jet mixer, a desorption tower, a hydrogen chloride cooler, a steam condenser and a waste water tank; the gas outlets of the acetylene pipeline and the hydrogen chloride pipeline are both communicated with the gas inlet of the mixer, and the gas outlet of the mixer is communicated with the gas inlet of the converter; the gas outlet of the converter is communicated with the gas inlet of the falling film absorber; an air outlet of the falling film absorber is communicated with an air inlet of the water washing tower, and a water outlet of the industrial water pipeline is communicated with a water inlet of the water washing tower; the air outlet of the water scrubber is communicated with the air inlet of the alkaline washing tower; the liquid outlet of the water washing tower is communicated with the liquid inlet of the dilute hydrochloric acid tank, the liquid outlet of the dilute hydrochloric acid tank is communicated with the liquid inlet of the dilute hydrochloric acid cooler, and the liquid outlet of the dilute hydrochloric acid cooler is communicated with the liquid inlet of the falling film absorber; a liquid outlet of the falling film absorber is communicated with a liquid inlet of the hydrochloric acid storage tank; the liquid outlet of the calcium chloride solution pipeline is communicated with the liquid inlet of the concentration tower; the liquid outlet of the concentration tower and the liquid outlet of the hydrochloric acid storage tank are both communicated with the liquid inlet of the jet mixer, and the liquid outlet of the jet mixer is communicated with the liquid inlet of the desorption tower; the gas outlet of the desorption tower is communicated with the gas inlet of the hydrogen chloride cooler; the gas outlet of the hydrogen chloride cooler is communicated with the gas inlet of the mixer; the gas outlet of the concentration tower is communicated with the gas inlet of the steam condenser, the water outlet of the steam condenser is communicated with the water inlet of the wastewater tank, and the water outlet of the wastewater tank is communicated with the water inlet of the washing tower.
Further, the device also comprises a mercury remover and a reaction gas cooler; the gas outlet of the converter is communicated with the gas inlet of the mercury remover, the gas outlet of the mercury remover is communicated with the gas inlet of the reaction gas cooler, and the gas outlet of the reaction gas cooler is communicated with the gas inlet of the falling film absorber.
Further, a liquid outlet of the dilute hydrochloric acid cooler is communicated with a liquid inlet of the water washing tower.
Further, a concentration reboiler is arranged at the bottom of the concentration tower; and a desorption reboiler is arranged at the bottom of the desorption tower.
Further, the system also comprises a liquid caustic soda pipeline, a caustic soda circulation tank, a precooler, a normal water seal tank, a gas holder and a reverse water seal tank; the liquid outlet of the liquid alkali pipeline and the water outlet of the industrial water pipeline are both communicated with the liquid inlet of the alkali circulation tank; a liquid outlet of the alkali circulation tank is communicated with a liquid inlet of the alkali washing tower; the air outlet of the alkaline tower is respectively communicated with the precooler and the air inlet of the positive water seal tank; the liquid outlet of the precooler is communicated with the liquid inlet of the alkali circulation tank; the gas outlet of the positive water seal tank is communicated with the gas inlet of the gas holder, the gas outlet of the gas holder is communicated with the gas inlet of the reverse water seal tank, and the gas outlet of the reverse water seal tank is communicated with the gas inlet of the alkaline tower.
Further, the system also comprises a liquid level sensor, an industrial water valve and a liquid caustic soda valve; the liquid level sensor is arranged in the alkali circulation tank; the industrial water valve is arranged on the industrial water pipeline at the liquid inlet of the alkali circulation tank; the liquid caustic soda pipeline at the liquid inlet of the caustic soda circulation tank is provided with the liquid caustic soda valve; the signal output end of the liquid level sensor is respectively connected with the signal input end of the controller through signals; and the signal output ends of the controllers are in signal connection with the signal input ends of the industrial water valve and the liquid caustic soda valve.
The utility model has the advantages that: 1. the utility model has simple connecting structure and easy realization; dilute hydrochloric acid washed by a water washing tower is concentrated by a falling film absorber and then is sent to a desorption tower to be analyzed into hydrogen chloride gas which is used as raw material gas to be recycled and sent to a mixer, so that the removal of the hydrogen chloride gas in the crude chloroethylene synthetic gas is realized on one hand, the recycling of hydrogen chloride resources is realized on the other hand, the production cost of enterprises is reduced, and the economic benefit of the enterprises is improved; 2. acid wastewater generated by steam generated by the concentration tower after being condensed by a steam condenser is sent to a water washing tower as washing water, and alkaline wastewater generated by gas exhausted by an alkaline washing tower after being condensed by a precooler is sent to an alkaline circulation tank as washing alkaline liquor, so that the recycling of water resources is realized, and the water consumption cost of enterprises is reduced; 3. the gas cabinet is arranged for temporarily storing the crude chloroethylene gas, when the system runs at a low load, the crude chloroethylene gas can return to the alkaline tower, the system pressure is maintained within a certain time, and the normal operation of the system is ensured; 4. the utility model realizes the automatic configuration of the washing alkali liquor of the alkaline tower, ensures that the alkali liquor configured in the alkali circulation tank conforms to the standard of the washing alkali liquor of the alkaline tower, saves the labor cost and saves time and labor.
Description of the drawings:
in order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to the drawings without creative efforts.
Fig. 1 is a schematic diagram of the overall connection structure of the system of the present invention.
The system comprises an acetylene pipeline 1, a hydrogen chloride pipeline 2, a mixer 3, a converter 4, a falling film absorber 5, a water scrubber 6, an industrial water pipeline 7, an alkaline washing tower 8, a dilute hydrochloric acid tank 9, a dilute hydrochloric acid cooler 10, a hydrochloric acid storage tank 11, a calcium chloride solution pipeline 12, a concentration tower 13, a jet mixer 14, a desorption tower 15, a hydrogen chloride cooler 16, a steam condenser 17, a wastewater tank 18, a mercury remover 19, a reaction gas cooler 20, a liquid caustic soda pipeline 21, an alkaline circulation tank 22, a precooler 23, a normal water seal tank 24, a gas cabinet 25, a reverse water seal tank 26, a liquid level sensor 27, an industrial water valve 28, a liquid caustic valve 29, a controller 30, a concentration reboiler 31 and a desorption reboiler 32.
The specific implementation mode is as follows:
as shown in fig. 1, a crude vinyl chloride purification system for realizing resource recovery is characterized by comprising an acetylene pipeline 1, a hydrogen chloride pipeline 2, a mixer 3, a converter 4, a falling film absorber 5, a water scrubber 6, an industrial water pipeline 7, an alkaline tower 8, a dilute hydrochloric acid tank 9, a dilute hydrochloric acid cooler 10, a hydrochloric acid storage tank 11, a calcium chloride solution pipeline 12, a concentration tower 13, a jet mixer 14, a desorption tower 15, a hydrogen chloride cooler 16, a steam condenser 17, a wastewater tank 18, a mercury remover 19, a reaction gas cooler 20, a liquid caustic soda pipeline 21, an alkaline circulation tank 22, a precooler 23, a normal water seal tank 24, a gas holder 25, a reverse water seal tank 26, a liquid level sensor 27, an industrial water valve 28 and a liquid caustic soda valve 29; the gas outlets of the acetylene pipeline 1 and the hydrogen chloride pipeline 2 are both communicated with the gas inlet of the mixer 3, and the gas outlet of the mixer 3 is communicated with the gas inlet of the converter 4; the gas outlet of the converter 4 is communicated with the gas inlet of a mercury remover 19, the gas outlet of the mercury remover 19 is communicated with the gas inlet of a reaction gas cooler 20, and the gas outlet of the reaction gas cooler 20 is communicated with the gas inlet of the falling film absorber 5; an air outlet of the falling film absorber 5 is communicated with an air inlet of the water washing tower 6, and a water outlet of the industrial water pipeline 7 is communicated with a water inlet of the water washing tower 6; the air outlet of the water scrubber 6 is communicated with the air inlet of the alkaline washing tower 8; the liquid outlet of the water washing tower 6 is communicated with the liquid inlet of a dilute hydrochloric acid tank 9, the liquid outlet of the dilute hydrochloric acid tank 9 is communicated with the liquid inlet of a dilute hydrochloric acid cooler 10, and the liquid outlet of the dilute hydrochloric acid cooler 10 is respectively communicated with the liquid inlets of the falling film absorber 5 and the water washing tower 6; a liquid outlet of the falling film absorber 5 is communicated with a liquid inlet of the hydrochloric acid storage tank 11; a liquid outlet of the calcium chloride solution pipeline 12 is communicated with a liquid inlet of the concentration tower 13, and a concentration reboiler 31 is arranged at the bottom of the concentration tower 13; the liquid outlet of the concentration tower 13 and the liquid outlet of the hydrochloric acid storage tank 11 are both communicated with the liquid inlet of the jet mixer 14, the liquid outlet of the jet mixer 14 is communicated with the liquid inlet of the desorption tower 15, and the bottom of the desorption tower 15 is provided with a desorption reboiler 32; the gas outlet of the desorption tower 15 is communicated with the gas inlet of the hydrogen chloride cooler 16; the gas outlet of the hydrogen chloride cooler 16 is communicated with the gas inlet of the mixer 3; the gas outlet of the concentration tower 13 is communicated with the gas inlet of the steam condenser 17, the water outlet of the steam condenser 17 is communicated with the water inlet of the waste water tank 18, and the water outlet of the waste water tank 18 is communicated with the water inlet of the water washing tower 6.
The liquid outlet of the liquid alkali pipeline 21 and the water outlet of the industrial water pipeline 7 are both communicated with the liquid inlet of the alkali circulation tank 22; the liquid outlet of the alkali circulation tank 22 is communicated with the liquid inlet of the alkali washing tower 8; an air outlet of the alkaline tower 8 is respectively communicated with an air inlet of the precooler 23 and an air inlet of the positive water seal tank 24; the liquid outlet of the precooler 23 is communicated with the liquid inlet of the alkali circulation tank 22; the air outlet of the positive water seal tank 24 is communicated with the air inlet of the air cabinet 25, the air outlet of the air cabinet 25 is communicated with the air inlet of the reverse water seal tank 26, and the air outlet of the reverse water seal tank 26 is communicated with the air inlet of the alkaline tower 8.
A liquid level sensor 27 is provided in the alkali circulation tank 22; an industrial water valve 28 is arranged on the industrial water pipeline 7 at the liquid inlet of the alkali circulation tank 22; a liquid caustic soda valve 29 is arranged on the liquid caustic soda pipeline 21 at the liquid inlet of the caustic soda circulation tank 22; the signal output end of the liquid level sensor 27 is respectively connected with the signal input end of the controller 30 through signals; the signal output ends of the controller 30 are connected with the signal input ends of the industrial water valve 28 and the liquid caustic soda valve 29 through signals.
The working principle is as follows:
the acetylene and the hydrogen chloride mixed in the mixer 3 are sent to a converter 4, the crude vinyl chloride synthesized by the converter 4 enters a mercury remover 19, the mercury is removed by using activated carbon in the mercury remover, the crude vinyl chloride enters a tube side of a reaction gas cooler 20, is cooled by cooling water on a shell side and then flows with dilute hydrochloric acid from a dilute hydrochloric acid cooler 10 to enter a falling film absorber 5, the dilute hydrochloric acid absorbs the hydrogen chloride in the crude vinyl chloride in the falling film absorber 5 and is concentrated, and the concentrated hydrochloric acid is sent to a hydrochloric acid storage tank 11. The crude chloroethylene passing through the falling film absorber 5 enters a water washing tower 6 to be in countercurrent contact with industrial water, dilute hydrochloric acid from a dilute hydrochloric acid cooler 10 and acidic wastewater in a wastewater tank 18, so that hydrogen chloride is removed; hydrochloric acid at the bottom of the water washing tower 6 enters a dilute hydrochloric acid tank 9, and the hydrochloric acid in the dilute hydrochloric acid tank 9 is cooled to 10 ℃ through a dilute hydrochloric acid cooler 10.
The washed crude vinyl chloride gas enters an alkaline tower 8, and 15% liquid caustic soda is used for removing hydrogen chloride and carbon dioxide again, namely the alkaline liquor in the alkaline circulation tank 22 is sent to the top end of the alkaline tower 8, and the crude vinyl chloride gas enters from the bottom of the alkaline tower 8; after hydrogen chloride and water are removed from the crude chloroethylene, a part of the crude chloroethylene enters a precooler 23 to be cooled, the cooled crude chloroethylene is sent to a subsequent rectification system to be continuously treated, and cooling water is recycled into an alkali circulation tank 22, so that the recycling of water resources is realized, and the water consumption cost of enterprises is reduced; the other part of the crude chloroethylene gas enters a gas holder 25 for temporary storage through a positive water seal tank 24; when the system operates at low load, the crude chloroethylene gas in the gas holder 25 can be returned to the alkaline washing tower 8 from the reverse water seal tank 26, and the system pressure is maintained within a certain time to ensure the normal operation of the system.
The alkali circulation tank 22 is one for use; the content of sodium carbonate in the washing lye in the alkali circulation tank 22 is manually detected, when the detected content of sodium carbonate reaches a set value, the washing lye in the alkali circulation tank 22 is stopped from being used, and the alkali circulation tank 22 is switched to another standby alkali circulation tank 22 with the washing lye.
When the washing alkali liquor is configured for the alkali circulation tank 22, the controller 30 firstly controls the industrial water valve 28 to be opened, the industrial water is added into the alkali circulation tank 22, the liquid level sensor 27 detects the change of the water level in the alkali circulation tank 22 at any time and transmits a signal to the controller 30, when the detected water level reaches a set value on the controller 30, the controller 30 controls the industrial water valve 28 to be closed, the liquid alkali valve 29 is opened, a certain amount of 32% of liquid alkali is added into the alkali circulation tank 22, and after the addition is finished, the controller 30 is started until the liquid alkali valve 29 is closed, so that the configuration of the washing alkali liquor is finished.
The dilute hydrochloric acid in the hydrochloric acid storage tank 11 and the calcium chloride solution concentrated from the concentration tower 13 are jointly fed into the jet mixer 14 to be mixed, and then are fed into the desorption tower 15, the mixed solution enters from the top of the desorption tower 15, under the heating of the desorption reboiler 32, the calcium chloride solution is used as a boiling breaker, the constant boiling point of the dilute hydrochloric acid is broken under certain temperature and pressure, the boiling point of the dilute hydrochloric acid solution is improved, in the process, the hydrogen chloride gas is stripped from the mixed solution of hydrochloric acid and calcium chloride, the hydrogen chloride gas is obtained at the tower top, after the hydrogen chloride gas is cooled and condensed by the hydrogen chloride cooler 16, the non-condensable hydrogen chloride gas is recycled as the raw material gas to be fed into the mixer 3 again, on one hand, the removal of the hydrogen chloride gas in the crude chloroethylene synthetic gas is realized, on the other hand, the recycling of hydrogen chloride resources is realized, and the production cost of enterprises is reduced, the economic benefit of enterprises is improved.
Dilute acid mixed solution containing calcium chloride obtained at the bottom of a desorption tower 15 is sent to a concentration tower 13, a concentration reboiler 31 is subjected to steam heating, a large amount of water vapor is generated and carries with the calcium chloride to be evaporated, the aim of concentrating the calcium chloride is achieved, the concentrated calcium chloride solution is sent to a jet mixer 14, discharged water vapor is fully condensed by a steam condenser 17, non-condensable gas is discharged into the atmosphere, acid wastewater is collected in a wastewater tank 18 and is sent to a water washing tower 6 as washing water at the later stage, the recycling of water resources is realized, and the water cost of enterprises is reduced; the utility model has simple connecting structure and easy realization.
The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the utility model, and any modifications, equivalents, improvements and the like that fall within the spirit and principle of the present invention are intended to be included therein.
Claims (6)
1. A crude chloroethylene purification system for realizing resource recovery is characterized by comprising an acetylene pipeline, a hydrogen chloride pipeline, a mixer, a converter, a falling film absorber, a water scrubber, an industrial water pipeline, an alkaline washing tower, a dilute hydrochloric acid tank, a dilute hydrochloric acid cooler, a hydrochloric acid storage tank, a calcium chloride solution pipeline, a concentration tower, a jet mixer, a desorption tower, a hydrogen chloride cooler, a steam condenser and a waste water tank;
the gas outlets of the acetylene pipeline and the hydrogen chloride pipeline are both communicated with the gas inlet of the mixer, and the gas outlet of the mixer is communicated with the gas inlet of the converter; the gas outlet of the converter is communicated with the gas inlet of the falling film absorber; an air outlet of the falling film absorber is communicated with an air inlet of the water washing tower, and a water outlet of the industrial water pipeline is communicated with a water inlet of the water washing tower; the air outlet of the water scrubber is communicated with the air inlet of the alkaline washing tower;
the liquid outlet of the water washing tower is communicated with the liquid inlet of the dilute hydrochloric acid tank, the liquid outlet of the dilute hydrochloric acid tank is communicated with the liquid inlet of the dilute hydrochloric acid cooler, and the liquid outlet of the dilute hydrochloric acid cooler is communicated with the liquid inlet of the falling film absorber; a liquid outlet of the falling film absorber is communicated with a liquid inlet of the hydrochloric acid storage tank;
the liquid outlet of the calcium chloride solution pipeline is communicated with the liquid inlet of the concentration tower; the liquid outlet of the concentration tower and the liquid outlet of the hydrochloric acid storage tank are both communicated with the liquid inlet of the jet mixer, and the liquid outlet of the jet mixer is communicated with the liquid inlet of the desorption tower; the gas outlet of the desorption tower is communicated with the gas inlet of the hydrogen chloride cooler; the gas outlet of the hydrogen chloride cooler is communicated with the gas inlet of the mixer;
the gas outlet of the concentration tower is communicated with the gas inlet of the steam condenser, the water outlet of the steam condenser is communicated with the water inlet of the wastewater tank, and the water outlet of the wastewater tank is communicated with the water inlet of the washing tower.
2. The crude vinyl chloride purification system for achieving resource recovery of claim 1, further comprising a mercury remover and a reaction gas cooler; the gas outlet of the converter is communicated with the gas inlet of the mercury remover, the gas outlet of the mercury remover is communicated with the gas inlet of the reaction gas cooler, and the gas outlet of the reaction gas cooler is communicated with the gas inlet of the falling film absorber.
3. The system for purifying crude vinyl chloride for realizing resource recovery as claimed in claim 1 or 2, wherein the liquid outlet of the dilute hydrochloric acid cooler is communicated with the liquid inlet of the water washing tower.
4. The crude vinyl chloride purification system for realizing resource recovery according to claim 1 or 2, wherein a concentration reboiler is arranged at the bottom of the concentration tower; and a desorption reboiler is arranged at the bottom of the desorption tower.
5. The crude vinyl chloride purification system for realizing resource recovery according to claim 1 or 2, further comprising a liquid caustic soda pipeline, a caustic soda circulation tank, a precooler, a normal water seal tank, a gas holder and a reverse water seal tank;
the liquid outlet of the liquid alkali pipeline and the water outlet of the industrial water pipeline are both communicated with the liquid inlet of the alkali circulation tank; a liquid outlet of the alkali circulation tank is communicated with a liquid inlet of the alkali washing tower; the air outlet of the alkaline tower is respectively communicated with the precooler and the air inlet of the positive water seal tank; the liquid outlet of the precooler is communicated with the liquid inlet of the alkali circulation tank; the gas outlet of the positive water seal tank is communicated with the gas inlet of the gas holder, the gas outlet of the gas holder is communicated with the gas inlet of the reverse water seal tank, and the gas outlet of the reverse water seal tank is communicated with the gas inlet of the alkaline tower.
6. The crude vinyl chloride purification system for realizing resource recovery of claim 5, further comprising a liquid level sensor, an industrial water valve and a liquid caustic soda valve; the liquid level sensor is arranged in the alkali circulation tank; the industrial water valve is arranged on the industrial water pipeline at the liquid inlet of the alkali circulation tank; the liquid caustic soda pipeline at the liquid inlet of the caustic soda circulation tank is provided with the liquid caustic soda valve;
the signal output end of the liquid level sensor is respectively connected with the signal input end of the controller through signals; and the signal output ends of the controllers are in signal connection with the signal input ends of the industrial water valve and the liquid caustic soda valve.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202121142514.2U CN215627707U (en) | 2021-05-25 | 2021-05-25 | Realize resource recovery's crude chloroethylene clean system |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202121142514.2U CN215627707U (en) | 2021-05-25 | 2021-05-25 | Realize resource recovery's crude chloroethylene clean system |
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