CN218130947U - System for removing organic matters in chloroacetic acid production tail gas - Google Patents
System for removing organic matters in chloroacetic acid production tail gas Download PDFInfo
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- CN218130947U CN218130947U CN202222121491.8U CN202222121491U CN218130947U CN 218130947 U CN218130947 U CN 218130947U CN 202222121491 U CN202222121491 U CN 202222121491U CN 218130947 U CN218130947 U CN 218130947U
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Abstract
The utility model relates to a desorption system of organic matter in chloroacetic acid production tail gas, it includes chloroacetic acid combination absorption tower, chloroacetic acid crystallizer and contaminated acid scrubbing tower, the liquid phase entry on chloroacetic acid combination absorption tower upper portion is the chloroacetic acid inlet, the gaseous phase entry of chloroacetic acid combination tower lower part is chloroacetic acid tail gas entry, the gaseous phase export switch-on chloroacetic acid crystallizer on chloroacetic acid combination absorption tower upper portion, the gaseous phase entry of chloroacetic acid crystallizer switch-on contaminated acid scrubbing tower lower part, the liquid phase entry on contaminated acid scrubbing tower upper portion is the hydrochloric acid inlet. The utility model discloses greatly reduced organic matter content in chloroacetic acid production tail gas, widened the application range of the hydrochloric acid that adopts tail gas to make to the desorption process can not produce a large amount of dirty acid, can reduce organic matter absorption to about 0.2% in the gaseous phase, and dirty sour output reduces to below 10% original, has apparent positive meaning to process optimization, green production.
Description
Technical Field
The utility model relates to a chemical industry tail gas treatment facility technical field specifically is a desorption system of organic matter in chloroacetic acid production tail gas.
Background
According to relevant data, the yield of chloroacetic acid in 2019 is about 76 million tons, the production process of chloroacetic acid generally adopts an acetic acid and acetic anhydride chlorination method, 1 mole of chloroacetic acid generates 1 mole of hydrogen chloride, the tail gas of chloroacetic acid contains hydrogen chloride, acetic acid, chloroacetic acid, dichloroacetic acid, chloroacetyl chloride, chlorine and the like, and the hydrogen chloride in the tail gas is usually recycled to prepare hydrochloric acid in the industry.
In the original chloroacetic acid production process, the tail gas enters a tail gas treatment device after being washed by an acetic acid and chloroacetic acid reaction kettle, the freezing point of chloroacetic acid is high, the content of organic matters in the tail gas is high and can reach about 2-3%, if hydrochloric acid is directly absorbed, the hydrochloric acid contains a large amount of organic matters, the subsequent use range of the hydrochloric acid is greatly reduced, generally, the saturated hydrochloric acid is used for washing and absorbing before absorbing salifying acid, the organic matters in a gas phase are washed into the hydrochloric acid, but the organic matters in the gas phase are large in amount, a large amount of contaminated acid is generated in a secondary working section, and the treatment difficulty is very high.
Chinese patent CN212632236U discloses a tail gas purification and recovery device for chloroacetic acid production, which includes a hydrochloric acid washing tower, a falling film absorption tower, a tail gas absorption tower and an alkali absorption device, which are sequentially arranged according to the tail gas flowing direction, wherein the hydrochloric acid washing tower is used for communicating with a tail gas source, and further includes a first liquid storage tank, the hydrochloric acid washing tower is provided with a first liquid outlet, and the first liquid outlet is communicated with the first liquid storage tank. The utility model discloses a have the efficiency of purifying chloroacetic acid production tail gas, but it has only handled the acetic acid organic matter in the tail gas, and still contains organic matters such as chloroacetic acid, dichloroacetic acid, chloroacetyl chloride in the present chloroacetic acid production tail gas usually, therefore this recovery unit is not complete enough to the organic matter purification in the chloroacetic acid production tail gas, influences the follow-up hydrochloric acid quality of taking tail gas to make.
SUMMERY OF THE UTILITY MODEL
The utility model provides a desorption system of organic matter in chloroacetic acid production tail gas to solve among the prior art chloroacetic acid tail gas organic matter and purify incompletely and produce the big technical problem of dirty sour volume.
In order to solve the technical problem, the utility model provides a technical scheme does:
the utility model relates to a desorption system of organic matter in chloroacetic acid production tail gas, it includes chloroacetic acid combination absorption tower, chloroacetic acid crystallizer and dirty sour scrubbing tower, the liquid phase entry on chloroacetic acid combination absorption tower upper portion is the chloroacetic acid inlet, the gaseous phase entry of chloroacetic acid combination tower lower part is chloroacetic acid tail gas entry, the gaseous phase export switch-on chloroacetic acid crystallizer on chloroacetic acid combination absorption tower upper portion, the gaseous phase entry of chloroacetic acid crystallizer switch-on dirty sour scrubbing tower lower part, the liquid phase entry on dirty sour scrubbing tower upper portion is the hydrochloric acid inlet.
The utility model discloses a chloroacetic acid combination absorption tower, let in chloroacetic acid combination absorption tower as the absorbent of gaseous phase organic matter during the use, belong to high boiling point acid because of chloroacetic acid, and balanced partial pressure in hydrogen chloride is lower, and according to the principle that the similarity is mutually soluble, organic matters such as acetic acid are great in the chloroacetic acid solubility, multistage absorption through chloroacetic acid combination absorption tower, other organic matter contents in the control absorbent, the relative volatility of organic matter in the hydrogen chloride has been reduced, after the washing absorption of chloroacetic acid, organic matter in the gaseous phase is basically dissolved in chloroacetic acid, remaining organic matter in the gaseous phase mainly is chloroacetic acid, the subsequent processing of being convenient for.
Preferably, the chloroacetic acid crystallizer is also communicated with a chloroacetic acid intermediate tank, the chloroacetic acid intermediate tank is communicated with a liquid phase inlet at the upper part of the chloroacetic acid combined absorption tower, and a first circulating pump is arranged between the chloroacetic acid intermediate tank and the liquid phase inlet at the upper part of the chloroacetic acid combined absorption tower. The chloroacetic acid can be recycled through the first circulating pump, waste is avoided, and the concept of green development in China is met.
Preferably, the chloroacetic acid combined absorption tower is provided with at least 1 group, and the waste acid washing tower is provided with at least 1 group.
Preferably, at least 2 sets of chloroacetic acid combined absorption towers are provided, and each chloroacetic acid combined absorption tower is connected in series.
Preferably, the chloroacetic acid crystallizers are arranged in 2 groups, and the 2 groups of chloroacetic acid crystallizers are arranged in parallel. Chloroacetic acid can be crystallized on a chloroacetic acid crystallizer, so in order to improve the efficiency, 2 groups of chloroacetic acid crystallizers need to be provided with one opening and one standby, and are switched for use according to pressure difference control; the cooling source of the chloroacetic acid crystallizer can use circulating water, low-temperature water or chilled water, and the lower the temperature is, the lower the content of chloroacetic acid in a gas phase is; the heat source for crystallizing and dissolving the chloroacetic acid crystallizer can adopt steam, hot water or other heat conducting oil and the like.
Preferably, the dirty acid washing towers are arranged in at least 2 groups, and the dirty acid washing towers are connected in series.
Preferably, the device also comprises a second circulating pump, a liquid inlet of the second circulating pump is communicated with a liquid phase outlet at the lower part of the sewage treatment tower, and a liquid outlet of the second circulating pump is communicated with a liquid phase inlet at the middle part of the sewage treatment tower.
Preferably, the device also comprises a third circulating pump, a liquid inlet of the third circulating pump is communicated with a liquid phase outlet at the lower part of the chloroacetic acid combined absorption tower, a liquid outlet of the third circulating pump is communicated with a liquid phase inlet at the middle part of the chloroacetic acid combined absorption tower, and a heat exchanger is arranged between the liquid phase inlet at the middle part of the chloroacetic acid combined absorption tower and the third circulating pump.
Preferably, the liquid outlet of the third circulating pump is also communicated with a chloroacetic acid discharge port, and the chloroacetic acid discharge port is communicated with the chloroacetic acid absorption liquid when in use.
Preferably, the liquid outlet of the second circulating pump is also communicated with a waste acid discharge port for discharging the redundant waste acid.
Adopt the utility model relates to a technical scheme compares with prior art, has following beneficial effect:
1. the utility model relates to a desorption system of organic matter in chloroacetic acid production tail gas can carry out the desorption to the organic matter in the chloroacetic acid production tail gas, and the content of organic matter in the greatly reduced chloroacetic acid production tail gas makes tail gas become the high hydrogen chloride gas of purity, has improved the hydrochloric acid quality that chloroacetic acid production tail gas produced, has widened the application scope of the hydrochloric acid who makes.
2. The utility model relates to a desorption system can adopt chloroacetic acid as the absorbent of gaseous phase organic matter in the chloroacetic acid tail gas, and chloroacetic acid can dissolve the organic matter in the gaseous phase, and the impurity in the tail gas through dirty sour scrubbing tower is chloroacetic acid, consequently compares in the dirty sour washing of tradition, and this system need not to use a large amount of hydrochloric acid to dissolve multiple impurity, just also can not produce a large amount of dirty sour, has reduced dirty sour treatment cost, has improved the economic nature of production.
3. The content of organic matter is 2 ~ 3% in the chloroacetic acid production tail gas, the utility model relates to a removal system uses chloroacetic acid to absorb organic matter in the hydrogen chloride, can reduce the organic matter absorption in the gaseous phase to about 0.2%, and the dirty sour output reduces to below 10% original, has increased the organic matter recovery volume in the gaseous phase, has reduced the manufacturing cost of chloroacetic acid, has reduced dirty sour treatment cost, has apparent positive meaning to process optimization, green production.
Drawings
Fig. 1 is a schematic structural diagram of a removal system for organic matters in tail gas in chloroacetic acid production.
In the figure: 1. the device comprises a chloroacetic acid combined absorption tower, 11, a chloroacetic acid liquid inlet, 12, a chloroacetic acid tail gas inlet, 2, a chloroacetic acid crystallizer, 3, a waste acid washing tower, 31, a hydrochloric acid liquid inlet, 32, a gas phase outlet, 4, a heat exchanger, 5, a chloroacetic acid intermediate tank, 6, a third circulating pump, 7, a first circulating pump, 8, a second circulating pump, 9, a waste acid discharge port, 10 and a chloroacetic acid discharge port.
Detailed Description
For further understanding of the present invention, the detailed description of the present invention is given in conjunction with the following embodiments, which are provided to illustrate the present invention but not to limit the scope of the present invention.
Referring to fig. 1, the utility model relates to a desorption system of organic matter in chloroacetic acid production tail gas, it includes chloroacetic acid combination absorption tower 1, chloroacetic acid crystallizer 2 and dirty acid scrubbing tower 3, the liquid phase entry on chloroacetic acid combination absorption tower 1 upper portion is chloroacetic acid inlet 11, the gas phase entry of chloroacetic acid combination tower 1 lower part is chloroacetic acid tail gas inlet 12, the gas phase export on chloroacetic acid combination absorption tower 1 upper portion switches on chloroacetic acid crystallizer 2, chloroacetic acid crystallizer 2 switches on the gas phase entry of dirty acid scrubbing tower 3 lower part, the liquid phase entry 32 on dirty acid scrubbing tower 3 upper portion is the hydrochloric acid inlet.
The removal system in the embodiment is a special removal system which adopts chloroacetic acid as an absorbent for organic matters in chloroacetic acid tail gas, and when the system is used, chloroacetic acid is introduced into a chloroacetic acid combined absorption tower, because chloroacetic acid belongs to high-boiling-point acid, the equilibrium partial pressure in hydrogen chloride is low, and according to the principle that similar substances are dissolved mutually, the solubility of organic matters such as acetic acid and the like in chloroacetic acid is high, the content of other organic matters in the absorbent is controlled through multistage absorption of the chloroacetic acid combined absorption tower, the relative volatility of the organic matters in hydrogen chloride is reduced, after the chloroacetic acid is washed and absorbed, the organic matters in a gas phase are basically dissolved in chloroacetic acid, and the organic matters remaining in the gas phase are mainly chloroacetic acid, so that subsequent treatment is facilitated.
Referring to fig. 1, the chloroacetic acid crystallizer 2 is further connected to a chloroacetic acid intermediate tank 5, the chloroacetic acid intermediate tank 5 is connected to a liquid phase inlet at the upper portion of the chloroacetic acid combined absorption tower 1, and a first circulation pump 7 is disposed between the chloroacetic acid intermediate tank 5 and the liquid phase inlet at the upper portion of the chloroacetic acid combined absorption tower. The chloroacetic acid can be recycled through the first circulating pump 7, waste is avoided, and the concept of green development in China is met. In the embodiment, the chloroacetic acid combined absorption tower 1 is provided with 1 group or a plurality of groups in series, and the waste acid washing tower is provided with 1 group or a plurality of groups in series. In the embodiment, 2 groups of chloroacetic acid crystallizers are arranged in parallel, chloroacetic acid can be crystallized on the chloroacetic acid crystallizers 2, and the chloroacetic acid crystallizers are required to be heated to recover chloroacetic acid after crystallization, so that in order to improve the efficiency, the 2 groups of chloroacetic acid crystallizers are required to be opened and prepared, and are switched to be used according to pressure difference control; the cooling source of the chloroacetic acid crystallizer 2 can use circulating water, low-temperature water or chilled water, and the lower the temperature is, the lower the content of chloroacetic acid in the gas phase is; the heat source for crystallizing and dissolving the chloroacetic acid crystallizer 2 can adopt steam, hot water or other heat conducting oil and the like.
Referring to fig. 1, the present embodiment further includes a second circulation pump 8, a liquid inlet of the second circulation pump 8 is connected to a liquid phase outlet at the lower portion of the waste water treatment tower 3, and a liquid outlet of the second circulation pump 8 is connected to a liquid phase inlet at the middle portion of the waste water treatment tower 3. This embodiment still includes third circulating pump 6, and the liquid inlet switch-on chloroacetic acid of third circulating pump 6 combines the liquid phase export of absorption tower 1 lower part, and the liquid outlet switch-on chloroacetic acid of third circulating pump 6 combines the liquid phase entry at 1 middle part of absorption tower, is equipped with heat exchanger 4 between the liquid phase entry at 1 middle part of chloroacetic acid combination absorption tower and the third circulating pump 6. A chloroacetic acid discharge port 10 is communicated with the liquid outlet of the third circulating pump 6, and the chloroacetic acid discharge port 10 needs to be communicated with the chloroacetic acid absorption liquid when in use. And a waste acid discharge port 9 is communicated with the liquid outlet of the second circulating pump 8 and is used for discharging redundant waste acid.
Adopt the utility model relates to a during organic matter in desorption system desorption chloroacetic acid tail gas, chloroacetic acid tail gas can be through the desorption purification of following three stage:
1) Chloroacetic acid combined absorption tower stage
Chloroacetic acid tail gas enters the chloroacetic acid combined absorption tower 1 through a chloroacetic acid tail gas inlet 12, a proper amount of fresh chloroacetic acid is added into the chloroacetic acid combined absorption tower 1 through a chloroacetic acid liquid inlet 11 according to the content of organic matters in the chloroacetic acid tail gas, and the two are subjected to gas-liquid mass transfer in the chloroacetic acid combined absorption tower 1. Chloroacetic acid is adopted as an absorbent for gas-phase organic matters, and is a high-boiling-point acid, the equilibrium partial pressure in hydrogen chloride is low, and according to the principle of similarity and compatibility, the solubility of organic matters such as acetic acid and the like in the chloroacetic acid is high, the contents of other organic matters in the absorbent are controlled through multistage absorption of the chloroacetic acid, the relative volatility of the organic matters in the hydrogen chloride is reduced, the organic matters in a gas phase are basically dissolved in the chloroacetic acid after the washing absorption of the chloroacetic acid, and the organic matters remaining in the gas phase are mainly the chloroacetic acid. Chloroacetic acid sprayed from the top of the chloroacetic acid combined absorption tower 1 can be recycled to the chloroacetic acid combined absorption tower 1 through a third circulating pump 6 for recycling, and meanwhile, the temperature of the chloroacetic acid combined absorption tower 1 can be controlled through a heat exchanger 4, and when the chloroacetic acid combined absorption tower cannot meet the utilization requirement, the chloroacetic acid is discharged from a chloroacetic acid discharge port 10 to the chloroacetic acid absorption liquid for absorption.
2) Chloroacetic acid crystallization stage
After chloroacetic acid tail gas is washed by chloroacetic acid, the content of chloroacetic acid in a gas phase is about 1 percent, as the freezing point of the chloroacetic acid is 55-65 ℃, the chloroacetic acid can form crystals on the inner surface of a chloroacetic acid crystallizer 2 after being cooled by circulating water, the difference between the saturated vapor pressure of the chloroacetic acid in a liquid phase and the saturated vapor pressure of the chloroacetic acid in a solid phase in hydrogen chloride is large, the content of the chloroacetic acid in the gas phase is reduced to be below 0.2 percent, and a large amount of organic matters in the gas phase are removed. The chloroacetic acid crystallized by condensation is dissolved by a heating mode and then recovered to the chloroacetic acid intermediate tank 5, and then is sent to the chloroacetic acid combined absorption tower 1 by a first circulating pump 7 for recycling.
3) Dirty acid scrubber stage
Chloroacetic acid tail gas passing through a chloroacetic acid combined absorption tower 1 and a chloroacetic acid crystallizer 2 is changed into hydrogen chloride gas with high purity, the hydrogen chloride gas contains a trace amount of chloroacetic acid, the hydrogen chloride gas enters a waste acid washing tower 3, saturated hydrochloric acid enters the waste acid washing tower 3 from a hydrochloric acid liquid inlet 31, the hydrogen chloride gas is washed at high temperature by the saturated hydrochloric acid, the chloroacetic acid in a gas phase is absorbed into the hydrochloric acid again to form waste acid, the content of the chloroacetic acid in the gas phase is reduced to 50ppm, and the gas phase, namely the pure hydrogen chloride gas, can be discharged from a gas phase outlet 32 and enters a tail gas absorption device to prepare high-quality hydrochloric acid with a large use range. Hydrochloric acid low in the waste acid washing tower is changed into waste acid through absorption, the hydrochloric acid can be conveyed to the middle of the waste acid washing tower through a second circulating pump for cyclic utilization, in order to reduce the loss amount of hydrogen chloride, the concentration of hydrochloric acid in the waste acid needs to be controlled within a certain range, the circulating temperature of the waste acid can be increased, a heat exchanger or no heat exchanger is arranged as required, the temperature can be increased by means of heat release of hydrochloric acid absorption, the content of chloroacetic acid in the waste acid needs to be controlled when the waste acid absorbs the chloroacetic acid, fresh hydrochloric acid needs to be continuously supplemented, and when the waste acid at the bottom of the waste acid washing tower cannot meet the use requirements, the waste acid is discharged to a waste acid treatment device from a waste acid discharge port 9.
Because of the absorptive impurity's of hydrochloric acid quantity is not big, the single and basically chloroacetic acid of impurity kind to the dirty sour also circulated use that produces, consequently compare in desorption system of the same kind, the utility model relates to a desorption system finally produces the volume of dirty sour and reduces greatly, for desorption system of the same kind below 10%.
A large amount of organic impurities in the chloroacetic acid tail gas are removed after the chloroacetic acid tail gas passes through the chloroacetic acid combined absorption tower, so that if the requirement on the content of the organic matters in the tail gas is not high, a chloroacetic acid crystallizer and a waste acid washing tower in the system can also be removed; the amount of the added fresh chloroacetic acid needs to be adjusted according to the amount of organic matters in the chloroacetic acid tail gas, the amount of the added saturated hydrochloric acid needs to be adjusted according to the amount of organic matters in the waste acid, and both the fresh chloroacetic acid and the saturated hydrochloric acid are added against the flowing direction of a gas phase to generate an absorption gradient and enhance the removal effect.
The present invention has been described in detail with reference to the embodiments, but the description is only for the preferred embodiments of the present invention and should not be construed as limiting the scope of the present invention. All the equivalent changes and improvements made according to the application scope of the present invention should still fall within the scope of the patent coverage of the present invention.
Claims (10)
1. A desorption system of organic matter in chloroacetic acid production tail gas which characterized in that: the device comprises a chloroacetic acid combined absorption tower, a chloroacetic acid crystallizer and a waste acid washing tower, wherein a liquid phase inlet at the upper part of the chloroacetic acid combined absorption tower is a chloroacetic acid liquid inlet, a gas phase inlet at the lower part of the chloroacetic acid combined absorption tower is a chloroacetic acid tail gas inlet, a gas phase outlet at the upper part of the chloroacetic acid combined absorption tower is communicated with the chloroacetic acid crystallizer, the chloroacetic acid crystallizer is communicated with a gas phase inlet at the lower part of the waste acid washing tower, and a liquid phase inlet at the upper part of the waste acid washing tower is a hydrochloric acid liquid inlet.
2. The system for removing organic matters in chloroacetic acid production tail gas according to claim 1, wherein: the chloroacetic acid crystallizer is also communicated with a chloroacetic acid intermediate tank, the chloroacetic acid intermediate tank is communicated with a liquid phase inlet at the upper part of the chloroacetic acid combined absorption tower, and a first circulating pump is arranged between the chloroacetic acid intermediate tank and the liquid phase inlet at the upper part of the chloroacetic acid combined absorption tower.
3. The system for removing organic matters in chloroacetic acid production tail gas according to claim 1, characterized in that: the chloroacetic acid combined absorption tower is at least provided with 1 group, and the waste acid washing tower is at least provided with 1 group.
4. The system for removing organic matters in chloroacetic acid production tail gas according to claim 1, characterized in that: at least 2 groups of chloroacetic acid combined absorption towers are arranged, and the chloroacetic acid combined absorption towers are connected in series.
5. The system for removing organic matters in chloroacetic acid production tail gas according to claim 1, characterized in that: the chloroacetic acid crystallizers are arranged in 2 groups, and the 2 groups of chloroacetic acid crystallizers are arranged in parallel.
6. The system for removing organic matters in chloroacetic acid production tail gas according to claim 1, wherein: the dirty acid scrubber is at least provided with 2 groups, and all the dirty acid scrubbers are connected in series.
7. The system for removing organic matters in chloroacetic acid production tail gas according to claim 1, characterized in that: the device also comprises a second circulating pump, wherein a liquid inlet of the second circulating pump is communicated with a liquid phase outlet at the lower part of the sewage treatment tower, and a liquid outlet of the second circulating pump is communicated with a liquid phase inlet at the middle part of the sewage treatment tower.
8. The system for removing organic matters in chloroacetic acid production tail gas according to claim 1, characterized in that: the device also comprises a third circulating pump, wherein a liquid inlet of the third circulating pump is communicated with a liquid phase outlet at the lower part of the chloroacetic acid combined absorption tower, a liquid outlet of the third circulating pump is communicated with a liquid phase inlet at the middle part of the chloroacetic acid combined absorption tower, and a heat exchanger is arranged between the liquid phase inlet at the middle part of the chloroacetic acid combined absorption tower and the third circulating pump.
9. The system for removing organic matters in chloroacetic acid production tail gas according to claim 8, characterized in that: the liquid outlet of the third circulating pump is also communicated with a chloroacetic acid discharge port.
10. The system for removing organic matters in chloroacetic acid production tail gas according to claim 7, characterized in that: the liquid outlet of the second circulating pump is also communicated with a waste acid discharge port.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202222121491.8U CN218130947U (en) | 2022-08-12 | 2022-08-12 | System for removing organic matters in chloroacetic acid production tail gas |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202222121491.8U CN218130947U (en) | 2022-08-12 | 2022-08-12 | System for removing organic matters in chloroacetic acid production tail gas |
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