CN107827728A - Based on the processing method for reclaiming chloroacetic monoxone heavy constituent - Google Patents
Based on the processing method for reclaiming chloroacetic monoxone heavy constituent Download PDFInfo
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- CN107827728A CN107827728A CN201711179456.9A CN201711179456A CN107827728A CN 107827728 A CN107827728 A CN 107827728A CN 201711179456 A CN201711179456 A CN 201711179456A CN 107827728 A CN107827728 A CN 107827728A
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- monoxone
- heavy constituent
- chloroacetic
- reclaiming
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- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/09—Preparation of carboxylic acids or their salts, halides or anhydrides from carboxylic acid esters or lactones
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Abstract
The invention belongs to chemical technology field, and in particular to a kind of based on the processing method for reclaiming chloroacetic monoxone heavy constituent.This method first adds water in monoxone heavy constituent, heating, reaction is hydrolyzed, then be evaporated under reduced pressure, obtains chloroethene aqueous acid, finally the raffinate after vacuum distillation is dissolved in water, then burns or alkali neutralisation treatment.Ethyl chloroacetate in monoxone heavy constituent is successfully hydrolyzed to monoxone, then by being evaporated under reduced pressure, obtain chloroethene aqueous acid by the present invention by controlling hydrolysis temperature, hydrolysis time and addition hydrolysis auxiliary agent.The present invention not only increases the utilization rate of raw material, reduces the generation of the three wastes, alleviates the environmental protection pressure of enterprise, while reduces the production cost of product.
Description
Technical field
The invention belongs to chemical technology field, and in particular to a kind of based on the processing for reclaiming chloroacetic monoxone heavy constituent
Method.
Background technology
Monoxone is a kind of important fine-chemical intermediate, is widely used in agricultural chemicals, medicine, dyestuff, detergents and cosmetic
The fields such as product, chemical reagent, food additives.But caused monoxone heavy constituent is that one kind is easily waved in process of production
Hair, hypertoxic, sticky waste liquid, have great destruction to environment, great threat are constituted to the life and health of the mankind.
At present, the processing mode for monoxone heavy constituent vinasse mainly has following three kinds：
1st, bioanalysis after first alkali neutralizes：In alkali and a large amount of alkali lye are needed, cost is higher, waste liquid residence time length, processing pond
Floor space is big, and treatment effect is unstable, is influenceed greatly by natural causes such as season, temperature, illumination.
2nd, as selling outside flammable burning heavy oil or steam burning disposal：It is narrower that approach is sold outside flammable burning heavy oil；Burning method is invested
Greatly, the occupied fund cycle is grown, and burns and the calorific value of rubbish there are certain requirements, typically cannot be below 5000kJ/kg, limit its
Application, burning can also produce pernicious gas, discharge carbon dioxide, the problems such as causing environmental pollution and greenhouse effects.
3rd, downstream product is produced using contained key component：The separation of product and impurity is main during production downstream product
Problem is wanted, while raw material availability is relatively low, therefore, monoxone heavy constituent waste liquid is unfavorable for producing downstream product.
Therefore, a kind of high treating effect of research and development, technique are needed badly simply based on the chloroacetic monoxone heavy constituent of recovery
Processing method.
The content of the invention
It is an object of the invention to provide a kind of technique is simple, cost is low, improve raw material availability based on recovery monoxone
Monoxone heavy constituent processing method.
Processing method of the present invention based on the chloroacetic monoxone heavy constituent of recovery, in monoxone heavy constituent first
Water is added, heating, reaction is hydrolyzed, then is evaporated under reduced pressure, chloroethene aqueous acid is obtained, finally adds the raffinate after vacuum distillation
Water dissolves, then burns or alkali neutralisation treatment.
Wherein：
Described hydrolysis is carried out in the presence of auxiliary agent is hydrolyzed, hydrolysis auxiliary agent be aluminium chloride, beryllium chloride, magnesium nitrate or
Scandium nitrate.
The quality of described hydrolysis auxiliary agent is the 1.0-2.5% of water quality.
Described monoxone heavy constituent, the mass ratio of water are 100:50-100, preferably 100:60-80.
Described is warming up to 80-100 DEG C.Temperature is less than 80 DEG C or higher than 100 DEG C, and hydrolysis effect is very poor, after hydrolysis
The content of the monoxone acetic acid esters contained in monoxone heavy constituent is higher.
Described hydrolysis time is 7-20h.Less than 7h, hydrolysis effect is bad, in the monoxone heavy constituent after hydrolysis
The content of the monoxone acetic acid esters contained is higher；It is relatively low higher than 20h, production efficiency.
The pressure of described vacuum distillation is that -0.090MPa pushes up warm highest control to -0.095MPa, during vacuum distillation and existed
Between 129-138 DEG C.
When the temperature of raffinate is 115-130 DEG C, 75-85 DEG C of water dissolving is added, then is burned or alkali neutralisation treatment.
Beneficial effects of the present invention are as follows：
In the prior art, directly monoxone heavy constituent is hydrolyzed it is relatively difficult because contained in monoxone heavy constituent
Acidic materials it is stronger, so be hydrolyzed to reversible reaction in acid condition, cause hydrolysis not thorough.
The present invention is by controlling hydrolysis temperature, hydrolysis time and addition hydrolysis auxiliary agent, successfully by monoxone heavy constituent
Ethyl chloroacetate be hydrolyzed to monoxone, then by being evaporated under reduced pressure, obtain chloroethene aqueous acid, finally will be residual after vacuum distillation
Liquid is dissolved in water, then carries out burning disposal or alkali neutralisation treatment, and biochemical wastewater treatment can be sent after alkali neutralisation treatment.When raffinate
When temperature is 115-130 DEG C, 75-85 DEG C of water dissolving is added, the material be advantageous in residual night fully dissolves.
By adding water in monoxone heavy constituent heating, reaction is hydrolyzed in the present invention, then is evaporated under reduced pressure, and obtains chlorine
Acetic acid aqueous solution, finally the raffinate after vacuum distillation is dissolved in water, then burned or alkali neutralisation treatment.Its essence is will be sticky
Monoxone in monoxone heavy constituent is fully recycled, and remaining raffinate is handled, and monoxone yield reaches 53.33%
More than.The utilization rate of raw material is not only increased, reduces the generation of the three wastes, alleviates the environmental protection pressure of enterprise, while reduces production
The production cost of product.
Brief description of the drawings
Fig. 1 is the process chart of the present invention.
Embodiment
The present invention is described further with reference to embodiments.
Embodiment 1
Take monoxone heavy constituent stoste 150g to add in 500mL three-necked flasks, amount of water 150g, add beryllium chloride 3g, magnetic force
It is gradually heated up being warming up to 80 DEG C under stirring, keeps hydrolysis 20h at 80 DEG C, filtering, continue to employ.
Monoxone heavy constituent solution 300g is added in 500mL three-necked flasks after taking hydrolysed filtrate, 185 DEG C of oil bath heatings, magnetic
It is evaporated under reduced pressure under power stirring under -0.095MPa pressure, top begins with liquid when warm 39 DEG C and distillated, and pushes up warm highest control 138
DEG C, stop reaction when pushing up temperature and dropping to 90 DEG C, weighing distillate is that the quality of chloroethene aqueous acid is 243.3g, wherein chloroethene
Chloroacetic content is 92.83g in aqueous acid.Now keep oil bath pan temperature-resistant, opened after raffinate is stirred under vacuum into 30min
Begin to cool, when raffinate is cooled to 120 DEG C, add stirring and dissolving 10min after 80 DEG C of distilled water 56g, burning.With monoxone
Heavy constituent stoste total amount meter, chloroacetic yield are 61.89%.
Embodiment 2
Monoxone heavy constituent stoste 100g is taken to add in 500mL three-necked flasks, amount of water 60g adds aluminium chloride 1g, and magnetic force stirs
Mix down and be gradually heated up being warming up to 90 DEG C, keep hydrolysis 7h at 90 DEG C, filtering, continue to employ.
Monoxone heavy constituent solution 160g is added in 500mL three-necked flasks after taking hydrolysed filtrate, 185 DEG C of oil bath heatings, magnetic
It is evaporated under reduced pressure under power stirring under -0.095MPa pressure, top begins with liquid when warm 40 DEG C and distillated, and pushes up warm highest control 130
DEG C, stop reaction when pushing up temperature and dropping to 90 DEG C, weighing distillate is that the quality of chloroethene aqueous acid is 111.1g, wherein chloroethene
Chloroacetic content is 53.33g in aqueous acid.Now keep oil bath pan temperature-resistant, opened after raffinate is stirred under vacuum into 30min
Begin to cool, when raffinate is cooled to 120 DEG C, add stirring and dissolving 10min after 85 DEG C of distilled water 46g, burning.With monoxone
Heavy constituent stoste total amount meter, chloroacetic yield are 53.33%.
Embodiment 3
Monoxone heavy constituent stoste 100g is taken to add in 500mL three-necked flasks, amount of water 80g adds magnesium nitrate 2g, and magnetic force stirs
Mix down and be gradually heated up being warming up to 90 DEG C, keep hydrolysis 7h at 90 DEG C, filtering, continue to employ.
Monoxone heavy constituent solution 180g is added in 500mL three-necked flasks after taking hydrolysed filtrate, 185 DEG C of oil bath heatings, magnetic
It is evaporated under reduced pressure under power stirring under -0.095MPa pressure, top begins with liquid when warm 40 DEG C and distillated, and pushes up warm highest control 130
DEG C, stop reaction when pushing up temperature and dropping to 90 DEG C, weighing distillate is that the quality of chloroethene aqueous acid is 132.3g, wherein chloroethene
Chloroacetic content is 54.00g in aqueous acid.Now keep oil bath pan temperature-resistant, opened after raffinate is stirred under vacuum into 30min
Begin to cool, when raffinate is cooled to 120 DEG C, add stirring and dissolving 10min after 85 DEG C of distilled water 46g, burning.With monoxone
Heavy constituent stoste total amount meter, chloroacetic yield are 54%.
Embodiment 4
Take monoxone heavy constituent stoste 100g to add in 500mL three-necked flasks, amount of water 100g, add aluminium chloride 2.5g, magnetic
It is gradually heated up being warming up to 90 DEG C under power stirring, keeps hydrolysis 8h at 90 DEG C, filtering, continue to employ.
Monoxone heavy constituent solution 200g is added in 500mL three-necked flasks after taking hydrolysed filtrate, 185 DEG C of oil bath heatings, magnetic
It is evaporated under reduced pressure under power stirring under -0.090MPa pressure, top begins with liquid when warm 40 DEG C and distillated, and pushes up warm highest control 130
DEG C, stop reaction when pushing up temperature and dropping to 90 DEG C, weighing distillate is that the quality of chloroethene aqueous acid is 154.1g, wherein chloroethene
Chloroacetic content is 60.53g in aqueous acid.Now keep oil bath pan temperature-resistant, opened after raffinate is stirred under vacuum into 30min
Begin to cool, when raffinate is cooled to 120 DEG C, add stirring and dissolving 10min after 80 DEG C of distilled water 46g, burning.With monoxone
Heavy constituent stoste total amount meter, chloroacetic yield are 60.53%.
Embodiment 5
Take monoxone heavy constituent stoste 100g to add in 500mL three-necked flasks, amount of water 100g, add scandium nitrate 1g, magnetic force
It is gradually heated up being warming up to 90 DEG C under stirring, keeps hydrolysis 14h at 90 DEG C, filtering, continue to employ.
Monoxone heavy constituent solution 200g is added in 500mL three-necked flasks after taking hydrolysed filtrate, 185 DEG C of oil bath heatings, magnetic
It is evaporated under reduced pressure under power stirring under -0.093MPa pressure, top begins with liquid when warm 40 DEG C and distillated, and pushes up warm highest control 132
DEG C, stop reaction when pushing up temperature and dropping to 90 DEG C, weighing distillate is that the quality of chloroethene aqueous acid is 151.6g, wherein chloroethene
Chloroacetic content is 58.21g in aqueous acid.Now keep oil bath pan temperature-resistant, opened after raffinate is stirred under vacuum into 30min
Begin to cool, when raffinate is cooled to 125 DEG C, add stirring and dissolving 10min after 75 DEG C of distilled water 46g, burning.With monoxone
Heavy constituent stoste total amount meter, chloroacetic yield are 58.21%.
Embodiment 6
Take monoxone heavy constituent stoste 100g to add in 500mL three-necked flasks, amount of water 70g, add aluminium chloride 1.5g, magnetic force
It is gradually heated up being warming up to 90 DEG C under stirring, keeps hydrolysis 7h at 90 DEG C, filtering, continue to employ.
Monoxone heavy constituent solution 170g is added in 500mL three-necked flasks after taking hydrolysed filtrate, 185 DEG C of oil bath heatings, magnetic
It is evaporated under reduced pressure under power stirring under -0.095MPa pressure, top begins with liquid when warm 40 DEG C and distillated, and pushes up warm highest control 129
DEG C, stop reaction when pushing up temperature and dropping to 90 DEG C, weighing distillate is that the quality of chloroethene aqueous acid is 161.0g, wherein chloroethene
Chloroacetic content is 65.01g in aqueous acid.Now keep oil bath pan temperature-resistant, opened after raffinate is stirred under vacuum into 30min
Begin to cool, when raffinate is cooled to 120 DEG C, add stirring and dissolving 10min after 85 DEG C of distilled water 46g, burning.With monoxone
Heavy constituent stoste total amount meter, chloroacetic yield are 65.01%.
Comparative example 1
By being heated to 80 DEG C and be changed to be heated to 70 DEG C in embodiment 1, remaining step is the same as embodiment 1.With chlorine
Acetic acid heavy constituent stoste total amount meter, chloroacetic yield are 33.25%.
Comparative example 2
By being heated to 80 DEG C and be changed to be heated to 110 DEG C in embodiment 1, remaining step is the same as embodiment 1.With chlorine
Acetic acid heavy constituent stoste total amount meter, chloroacetic yield are 32.36%.
Comparative example 3
Hydrolysis 20h in embodiment 1 is changed to hydrolysis 25h, remaining step is the same as embodiment 1.With monoxone weight
Component stoste total amount meter, chloroacetic yield are 33.72%.
Comparative example 4
Hydrolysis 20h in embodiment 1 is changed to hydrolysis 6h, remaining step is the same as embodiment 1.Recombinated with monoxone
Divide stoste total amount meter, chloroacetic yield is 34.58%.
Comparative example 5
Beryllium chloride is added without in embodiment 1, remaining step is the same as embodiment 1.In terms of monoxone heavy constituent stoste total amount, chloroethene
The yield of acid is 31.62%.
The content of each composition is as follows in monoxone heavy constituent stoste in 1-6 of the embodiment of the present invention and comparative example 1-5：
Dichloroacetic acid：1.235%；Hydroxyacetic acid：1.200%；Acetic acid：1.243%, monoxone：54.174%, monoxone
Acetic acid esters 40.00%, impurity：2.148%；
After water separation in monoxone heavy constituent after embodiment 1 is hydrolyzed, the content of each composition is as follows：
Dichloroacetic acid：1.082%；Hydroxyacetic acid：23.004%；Acetic acid：1.600%, monoxone：73.752%, chloroethene
Sour acetic acid esters 0.00%, impurity：0.562%.
After water separation in monoxone heavy constituent after embodiment 2 is hydrolyzed, the content of each composition is as follows：
Dichloroacetic acid：1.033%；Hydroxyacetic acid：22.904%；Acetic acid：1.594%, monoxone：73.832%, chloroethene
Sour acetic acid esters 0.00%, impurity：0.637%.
After water separation in monoxone heavy constituent after embodiment 3 is hydrolyzed, the content of each composition is as follows：
Dichloroacetic acid：1.042%；Hydroxyacetic acid：23.095%；Acetic acid：1.588%, monoxone：73.690%, chloroethene
Sour acetic acid esters 0.00%, impurity：0.585%.
After water separation in monoxone heavy constituent after embodiment 4 is hydrolyzed, the content of each composition is as follows：
Dichloroacetic acid：1.075%；Hydroxyacetic acid：22.893%；Acetic acid：1.531%, monoxone：72.853%, chloroethene
Sour acetic acid esters 0.00%, impurity：1.648%.
After water separation in monoxone heavy constituent after embodiment 5 is hydrolyzed, the content of each composition is as follows：
Dichloroacetic acid：1.103%；Hydroxyacetic acid：23.015%；Acetic acid：1.624%, monoxone：73.593%, chloroethene
Sour acetic acid esters 0.00%, impurity：0.665%.
After water separation in monoxone heavy constituent after embodiment 6 is hydrolyzed, the content of each composition is as follows：
Dichloroacetic acid：1.089%；Hydroxyacetic acid：22.652%；Acetic acid：1.569%, monoxone：73.878%, chloroethene
Sour acetic acid esters 0.00%, impurity：0.812%.
After water separation in monoxone heavy constituent after comparative example 1 is hydrolyzed, the content of each composition is as follows：
Dichloroacetic acid：1.084%；Hydroxyacetic acid：11.146%；Acetic acid：1.599%, monoxone：62.460%, chloroethene
Sour acetic acid esters 23.150%, impurity：0.561%.
After water separation in monoxone heavy constituent after comparative example 2 is hydrolyzed, the content of each composition is as follows：
Dichloroacetic acid：1.083%；Hydroxyacetic acid：10.537%；Acetic acid：1.598%, monoxone：63.276%, chloroethene
Sour acetic acid esters 22.943%, impurity：0.563%.
After water separation in monoxone heavy constituent after comparative example 3 is hydrolyzed, the content of each composition is as follows：
Dichloroacetic acid：1.082%；Hydroxyacetic acid：13.264%；Acetic acid：1.602%, monoxone：61.626%, chloroethene
Sour acetic acid esters 21.866%, impurity：0.560%.
After water separation in monoxone heavy constituent after comparative example 4 is hydrolyzed, the content of each composition is as follows：
Dichloroacetic acid：1.080%；Hydroxyacetic acid：12.855%；Acetic acid：1.603%, monoxone：61.685%, chloroethene
Sour acetic acid esters 22.216%, impurity：0.561%.
After water separation in monoxone heavy constituent after comparative example 5 is hydrolyzed, the content of each composition is as follows：
Dichloroacetic acid：1.083%；Hydroxyacetic acid：11.982%；Acetic acid：1.597%, monoxone：59.125%, chloroethene
Sour acetic acid esters 25.649%, impurity：0.564%.
From above-mentioned data it can be found that when reaction condition is respectively heat temperature raising less than 80 DEG C or higher than 100 DEG C, hydrolysis
Between less than 7h or higher than 20h, be added without hydrolysis auxiliary agent when, hydrolysis it is not thorough, effect is poor, contains in the monoxone heavy constituent after hydrolysis
The content of some monoxone acetic acid esters is higher.Again by being evaporated under reduced pressure, the chloroacetic amount distilled is also just reduced, so that
Obtain chloroacetic low yield.
Claims (9)
- It is 1. a kind of based on the processing method for reclaiming chloroacetic monoxone heavy constituent, it is characterised in that：In monoxone heavy constituent Water is first added, heats up, reaction is hydrolyzed, then is evaporated under reduced pressure, chloroethene aqueous acid is obtained, finally by the raffinate after vacuum distillation It is dissolved in water, then burns or alkali neutralisation treatment.
- It is 2. according to claim 1 based on the processing method for reclaiming chloroacetic monoxone heavy constituent, it is characterised in that：Institute The hydrolysis stated is carried out in the presence of auxiliary agent is hydrolyzed, and hydrolysis auxiliary agent is aluminium chloride, beryllium chloride, magnesium nitrate or scandium nitrate.
- It is 3. according to claim 2 based on the processing method for reclaiming chloroacetic monoxone heavy constituent, it is characterised in that：Institute The quality for the hydrolysis auxiliary agent stated is the 1.0-2.5% of water quality.
- It is 4. according to claim 1 based on the processing method for reclaiming chloroacetic monoxone heavy constituent, it is characterised in that：Institute The monoxone heavy constituent stated, the mass ratio of water are 100:50-100.
- It is 5. according to claim 4 based on the processing method for reclaiming chloroacetic monoxone heavy constituent, it is characterised in that：Institute The monoxone heavy constituent stated, the mass ratio of water are 100:60-80.
- It is 6. according to claim 1 based on the processing method for reclaiming chloroacetic monoxone heavy constituent, it is characterised in that：Institute That states is warming up to 80-100 DEG C.
- It is 7. according to claim 1 based on the processing method for reclaiming chloroacetic monoxone heavy constituent, it is characterised in that：Institute The hydrolysis time stated is 7-20h.
- It is 8. according to claim 1 based on the processing method for reclaiming chloroacetic monoxone heavy constituent, it is characterised in that：Institute The pressure for the vacuum distillation stated be -0.090MPa pushed up to -0.095MPa, during vacuum distillation warm highest control 129-138 DEG C it Between.
- It is 9. according to claim 1 based on the processing method for reclaiming chloroacetic monoxone heavy constituent, it is characterised in that：When When the temperature of raffinate is 115-130 DEG C, 75-85 DEG C of water dissolving is added, then is burned or alkali neutralisation treatment.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110452112A (en) * | 2018-12-03 | 2019-11-15 | 山东民基化工有限公司 | The catalytic hydrogenation treatment technique of chloro-pivalyl chloride distillation residual liquid |
| CN111253243A (en) * | 2020-03-11 | 2020-06-09 | 莘县华祥盐化有限公司 | Treatment method for heavy components in chloroacetic acid rectification residues |
| CN114835575A (en) * | 2022-05-27 | 2022-08-02 | 成武县晨晖环保科技有限公司 | Method for producing chloroacetic acid mixed acid and trichloro-acetyl chloride by using residues in chloroacetyl chloride production process |
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| EP2518043A1 (en) * | 2011-04-29 | 2012-10-31 | Lonza Ltd. | Process for the production of 4-chloroacetyl chloride, 4-chloroacetic acid esters, amides and imides |
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| EP2518043A1 (en) * | 2011-04-29 | 2012-10-31 | Lonza Ltd. | Process for the production of 4-chloroacetyl chloride, 4-chloroacetic acid esters, amides and imides |
| CN103922916A (en) * | 2014-04-30 | 2014-07-16 | 中国天辰工程有限公司 | Chloroacetic acid chlorination mother solution treatment method |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110452112A (en) * | 2018-12-03 | 2019-11-15 | 山东民基化工有限公司 | The catalytic hydrogenation treatment technique of chloro-pivalyl chloride distillation residual liquid |
| CN110452112B (en) * | 2018-12-03 | 2022-03-25 | 山东民基新材料科技有限公司 | Catalytic hydrogenation treatment process for chloro pivaloyl chloride rectification residual liquid |
| CN111253243A (en) * | 2020-03-11 | 2020-06-09 | 莘县华祥盐化有限公司 | Treatment method for heavy components in chloroacetic acid rectification residues |
| CN114835575A (en) * | 2022-05-27 | 2022-08-02 | 成武县晨晖环保科技有限公司 | Method for producing chloroacetic acid mixed acid and trichloro-acetyl chloride by using residues in chloroacetyl chloride production process |
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