CN101575281A - Chloroacetic acid producing method and reaction equipment thereof - Google Patents
Chloroacetic acid producing method and reaction equipment thereof Download PDFInfo
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- CN101575281A CN101575281A CNA2009100745259A CN200910074525A CN101575281A CN 101575281 A CN101575281 A CN 101575281A CN A2009100745259 A CNA2009100745259 A CN A2009100745259A CN 200910074525 A CN200910074525 A CN 200910074525A CN 101575281 A CN101575281 A CN 101575281A
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- acetic acid
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- acid
- chlorine
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- 238000006243 chemical reaction Methods 0.000 title claims abstract description 43
- FOCAUTSVDIKZOP-UHFFFAOYSA-N chloroacetic acid Chemical compound OC(=O)CCl FOCAUTSVDIKZOP-UHFFFAOYSA-N 0.000 title claims abstract description 35
- 238000000034 method Methods 0.000 title claims abstract description 23
- 229940106681 chloroacetic acid Drugs 0.000 title claims abstract description 16
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 claims abstract description 76
- 239000000460 chlorine Substances 0.000 claims abstract description 32
- 229910052801 chlorine Inorganic materials 0.000 claims abstract description 32
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims abstract description 31
- 238000004519 manufacturing process Methods 0.000 claims abstract description 20
- WFDIJRYMOXRFFG-UHFFFAOYSA-N acetic acid anhydride Natural products CC(=O)OC(C)=O WFDIJRYMOXRFFG-UHFFFAOYSA-N 0.000 claims abstract description 16
- 238000005660 chlorination reaction Methods 0.000 claims abstract description 16
- 238000010992 reflux Methods 0.000 claims abstract description 15
- WETWJCDKMRHUPV-UHFFFAOYSA-N acetyl chloride Chemical compound CC(Cl)=O WETWJCDKMRHUPV-UHFFFAOYSA-N 0.000 claims abstract description 13
- 239000012346 acetyl chloride Substances 0.000 claims abstract description 13
- 239000007788 liquid Substances 0.000 claims abstract description 12
- 239000000376 reactant Substances 0.000 claims abstract description 8
- 238000004821 distillation Methods 0.000 claims abstract description 7
- 238000000926 separation method Methods 0.000 claims abstract description 7
- 239000011521 glass Substances 0.000 claims description 13
- 239000012717 electrostatic precipitator Substances 0.000 claims description 5
- 238000010899 nucleation Methods 0.000 claims description 4
- 230000006911 nucleation Effects 0.000 claims description 4
- 230000002269 spontaneous effect Effects 0.000 claims description 4
- 239000004033 plastic Substances 0.000 claims description 3
- 238000012423 maintenance Methods 0.000 claims description 2
- 238000012856 packing Methods 0.000 claims description 2
- 238000010792 warming Methods 0.000 claims description 2
- JXTHNDFMNIQAHM-UHFFFAOYSA-N dichloroacetic acid Chemical compound OC(=O)C(Cl)Cl JXTHNDFMNIQAHM-UHFFFAOYSA-N 0.000 abstract description 34
- 229960005215 dichloroacetic acid Drugs 0.000 abstract description 17
- 239000000047 product Substances 0.000 abstract description 15
- 239000012535 impurity Substances 0.000 abstract description 4
- 239000007795 chemical reaction product Substances 0.000 abstract description 3
- 239000002253 acid Substances 0.000 abstract 4
- 230000009286 beneficial effect Effects 0.000 abstract 1
- 210000003298 dental enamel Anatomy 0.000 abstract 1
- 239000012530 fluid Substances 0.000 abstract 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 239000006227 byproduct Substances 0.000 description 3
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 3
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 239000005864 Sulphur Substances 0.000 description 2
- 238000010923 batch production Methods 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 239000013078 crystal Substances 0.000 description 2
- 238000002425 crystallisation Methods 0.000 description 2
- 230000007812 deficiency Effects 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 239000000843 powder Substances 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 150000008065 acid anhydrides Chemical class 0.000 description 1
- 230000004913 activation Effects 0.000 description 1
- 239000013543 active substance Substances 0.000 description 1
- 239000003905 agrochemical Substances 0.000 description 1
- 239000012752 auxiliary agent Substances 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000005119 centrifugation Methods 0.000 description 1
- 125000001309 chloro group Chemical group Cl* 0.000 description 1
- NEHMKBQYUWJMIP-UHFFFAOYSA-N chloromethane Chemical compound ClC NEHMKBQYUWJMIP-UHFFFAOYSA-N 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000001143 conditioned effect Effects 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 239000000975 dye Substances 0.000 description 1
- 238000005194 fractionation Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 1
- 239000003317 industrial substance Substances 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000012452 mother liquor Substances 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000007747 plating Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 230000036632 reaction speed Effects 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 235000013599 spices Nutrition 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000000967 suction filtration Methods 0.000 description 1
- 239000004753 textile Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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Abstract
The invention provides a chloroacetic acid producing method and reaction equipment thereof; the producing method comprises the steps of: adding acetic acid and acetic anhydride which is equivalent to 10 to 15 percent of acetic acid into a reaction kettle, raising the temperature to 80 to 100 DEG C and keeping the temperature, introducing chlorine under normal pressure for chlorination with the aid of microwaves, distilling acetyl chloride and chloroactic acid liquid from the reaction products by the reduced pressure distillation, putting the chloroactic acid liquid into a soft container and causing the chloroactic acid liquid to crystallize naturally in shaking state. The reaction equipment comprises a reaction kettle provided with an enamel lining and a reflux condenser; the reaction kettle is internally provided with a chlorine pipe which is externally sleeved with a fluid director; a microwave generator is arranged at the end opening of the reaction kettle; an emission head of the microwave generator irradiates reactants in the reaction kettle. The invention has simple technology, safe and reliable equipment, low cost, short production period, high yield and high quality of chloroactic acid products with a purity rate higher than 99.5 percent. The invention reduces the production of an impurity of dichloroacetic acid, thus saving a separation process and being beneficial to the environment protection.
Description
Technical field
The invention belongs to the production of chloroacetic acid technical field, relate to a kind of chloroacetic method and apparatus of under the microwave-assisted effect, producing specifically.
Background technology
Mono Chloro Acetic Acid is a kind of important organic fine industrial chemicals, is widely used in fields such as agricultural chemicals, medicine, dyestuff, oil field chemical, papermaking chemical product, textile auxiliary agent, tensio-active agent, plating, spices and essence.Along with progress of science and technology and development, the Application Areas that Mono Chloro Acetic Acid is new will progressively obtain exploitation, and production of chloroacetic acid and market outlook are very good.Producing chloroacetic method both at home and abroad at present mainly is the acetic acid catalytic chlorination process, is divided into batch production and serialization and produces two kinds.Batch production technology generally is catalyzer with the SULPHUR POWDER, controlling its consumption is 3% (mass percent) of acetic acid total amount, the two-stage tandem chlorination is adopted in reaction, the main reaction still is logical chlorine under 90 ℃, control reaction temperature is 96-100 ℃, the secondary reacting kettle temperature of reaction is 85-90 ℃, is reaction end when reaction end density is 1.35.Insulation reaction adds the circulating mother liquor crystallisation by cooling after 1 hour, add crystal seed at the above 1-2 of zero pour ℃, slowly cools to about 25 ℃, obtains product through suction filtration or centrifugation.Though this method production technique is simple, but consume high, yield poorly, products obtained therefrom is second-rate, and the production cycle is long, cost height, three-waste pollution are serious, the catalyzer SULPHUR POWDER is not only polluted major product, and also contaminating by-products hydrochloric acid also causes the obstruction of pipe-line equipment sometimes, produce and often occur making the range of application of product be restricted unusually.
The applicant number produces chloroacetic technology and equipment for the patent of invention of CN1231448C discloses a kind of High Temperature High Pressure at Granted publication.This technology is: add acetic acid and the aceticanhydride that is equivalent to acetic acid 10～15% in reactor, maintain the temperature at 80～200 ℃, be forced into 0.8～4MPa, feed chlorine and carry out chlorination reaction, with the fractionation by distillation in separation column of the chlorated liquid in the reactor, still liquid is cooled to 70～80 ℃, stirs spontaneous nucleation in the inclosure flexible container and is the Mono Chloro Acetic Acid product.This technology is simple, and device structure is reasonable, is easy to temperature control, flexible and convenient operation.But the deficiency of this patent is, reactant can not react completely, when being reacted to acetic acid theoretical value 70～80%, need stop, and follow reaction also to produce 2% dichloro acetic acid impurity, this makes troubles not only for the product separation at rear portion, increases processing cost, also environment is caused severe contamination, influence quality product.
Summary of the invention
For overcoming above-mentioned the deficiencies in the prior art, the invention provides a kind of method of production of chloroacetic acid, effectively suppress by-product dichloroacetic acid and produce, make the acetic acid chlorination reaction rapidly, fully, reaction product purity height, quality are good, and the conversion unit of this method of a kind of effective realization is provided simultaneously.
The method of production of chloroacetic acid provided by the present invention is: add acetic acid and the aceticanhydride that is equivalent to acetic acid 10～15% in reactor, be warming up to 80～100 ℃ and maintenance temperature, normal pressure feeds chlorine and carries out chlorination reaction, carries out product separation after reaction finishes.Described chlorination reaction is carried out under the microwave power-assisted, and the wavelength of described microwave is 5～20cm.
Described product separation adopts the method for underpressure distillation, and Acetyl Chloride 98Min. of telling and Mono Chloro Acetic Acid liquid with the chloroacetic acid solution flexible container of packing into, are placed on the vibrations crystallizer spontaneous nucleation under vibrating state.Described flexible container is selected the woven bag of inner lining plastic bag, does not get rid of other flexible container.Vibrating crystallizer is common vibrations equipment as vibrations bed, spring electromagnetic shaker.
For realizing the method for described production of chloroacetic acid, conversion unit provided by the invention comprises: the reactor of band glass lining, and reflux exchanger is provided with chlorine tube in the reactor, and the reactor skin is provided with the temperature control chuck.A microwave generator is installed at reactor end opening place, and the emitting head of described microwave generator sees through the reactant of the polyfluortetraethylene plate orientating reaction still inside of reactor device bottom.Except that polyfluortetraethylene plate, use the material of other penetrable microwave also to belong to protection scope of the present invention in the reactor bottom.
Described chlorine tube is a Glass tubing, and the bottom of Glass tubing is with reinforced pipe.In the described reactor director is housed, the structure of described director is: with the concentric two of chlorine tube open tubes, be installed in the bottom of chlorine tube, the emission port of microwave generator is aimed at the end opening of director.The preferred glass pipe is a director.For reducing and preventing that acetic acid and Acetyl Chloride 98Min. run damage in the reflux course in reflux course, electrostatic precipitator is housed on the top of reflux exchanger.
Goal of the invention is to produce the major product Mono Chloro Acetic Acid to greatest extent, the least possible generation impurity by-product dichloroacetic acid.Studies show that, when forming dichloro acetic acid, there is the strong angle of a pair of chemical bond to change, the angle of two carbon chlorine keys that is dichloro acetic acid is greater than the angle of two hydrocarbon keys on the former acetic acid methyl, illustrate that two chlorine atoms of dichloro acetic acid are to finish substitution reaction sequentially, and second chlorine will change bond angle when finishing reaction, require the expenditure of energy and the time, the present invention utilizes this character of acetic acid chlorination reaction to carry out improved.Microwave can greatly increase the kinetic energy of polar molecule, and the energy that makes molecule is accelerated chemical reaction velocity considerably beyond activation energy.When forming dichloro acetic acid, changing strong angle needs elapsed time, and it is inoperative that microwave changes the time that is consumed to strong angle.Generation Mono Chloro Acetic Acid and dichloro acetic acid are competing reactions in the acetic acid chlorination process, dichloro acetic acid is owing to be subjected to the restriction that strong angle changes required time, after adopting the microwave power-assisted, the speed that dichloro acetic acid generates is not accelerated, therefore the speed of response that generates dichloro acetic acid makes dichloro acetic acid generate and levels off to zero well below generating chloroacetic speed of response.
The present invention adopts the microwave power-assisted to produce Mono Chloro Acetic Acid, because chloroacetic formation speed has been accelerated in the effect of microwave, suppress the generation of side reaction product dichloro acetic acid simultaneously, reactant in the still can react completely, acetic acid chlorating speed of response and selectivity have been improved, the Mono Chloro Acetic Acid product purity that generates can reach more than 99.5%, only contains the dichloro acetic acid of trace, directly reaches specification of quality without separating separating treatment.Adopt mode of vibration to carry out crystallization, process is simple, and the Mono Chloro Acetic Acid crystalline particle of production is tiny, epigranular, good stability.Chlorine tube overcoat reinforced pipe and use director make chlorine fully contact with acetic acid, are convenient to the zone that microwave rf generator concentrates irradiation reaction to carry out simultaneously, help fast reaction speed, effectively utilize microwave rf generator.On the top of reflux exchanger electrostatic precipitator is installed, reactant acetic acid in the reflux course and catalyst acetyl chloride are all condensed and returns reactor, avoid and minimizing is chlorinated hydrogen and carries secretly and run damage.Compared with prior art, technology of the present invention is simple, and device security is reliable, and production cost is low, and is with short production cycle, the Mono Chloro Acetic Acid productive rate height of production, good product quality.Reduce the generation of impurity dichloro acetic acid, saved sepn process, helped environment protection.
Description of drawings
Fig. 1 is a conversion unit structural representation of the present invention;
Fig. 2 is chlorine tube and director structural representation.
Among the figure:
1-reflux exchanger, 2-chlorine tube, 3-reactor, 4-temperature control chuck, 5-director, 6-microwave generator, 7-reinforced pipe.
Embodiment
The chloroacetic conversion unit of production of the present invention as shown in Figure 1, comprise the reactor 3 of being with glass lining, reflux exchanger 1 is provided with chlorine tube 2 in the reactor, chlorine tube is a glass round tube, be with reinforced pipe 7 in the bottom of glass round tube, reinforced pipe also is a Glass tubing, and chlorine tube outer has concentric director 5, and director is round Glass tubing, director is fixedly mounted on the bottom of chlorine tube, and the lower end of chlorine tube and reinforced pipe slightly is longer than in the director lower end.The reactor skin is provided with temperature control chuck 4, is used for conditioned reaction still temperature, and used medium is steam or water.A microwave generator 6 is installed at reactor end opening place, and the emitting head of microwave generator sees through the lower end of polyfluortetraethylene plate orientating reaction still internal flow director 5 on the reactor wall.Reflux exchanger is heat-eliminating medium with water, and electrostatic precipitator is equipped with on the top of reflux exchanger.Supporting equipment shakes crystallizer in addition, the underpressure distillation device.
Production processes of chloroacetic acid is: the aceticanhydride that adds acetic acid and be equivalent to acetic acid 12% to reactor 3, can select to add 5% Acetyl Chloride 98Min., catalyzer as initial reaction, pressure is normal pressure, feed steam to temperature control chuck 4, by reactant to 85 ± 5 in the steam cycle reacting by heating still ℃, constant temperature then, feed chlorine by chlorine tube 2 and carry out chlorination reaction, start microwave generator simultaneously, the polyfluortetraethylene plate that sees through reactor end opening place is to the director launched microwave, and the wavelength of microwave is 10cm.Because chlorination reaction is thermopositive reaction, stop heating after the reaction beginning, this feeds the cold water cooling to chuck, regulates the flow velocity of water coolant, 85 ± 5 ℃ of control reaction temperature.After feeding chlorine, chlorine is from the outlet ejection of chlorine tube 2 lower ends, upwards roll at the reinforced pipe of chlorine tube and the space between the director 5, driving acetic acid and catalyst acetyl chloride upwards flows, form the gas-to-liquid contact interface, chlorine injects continuously and drives liquid circulation in the still, increases the chance of reactant contact.The acetic acid chlorination reaction generates Mono Chloro Acetic Acid and hydrogenchloride, and the catalyzer of chlorination reaction is an Acetyl Chloride 98Min., and Acetyl Chloride 98Min. is generated by acid anhydrides and hcl reaction, and the total amount of Acetyl Chloride 98Min. does not change in the reaction process.Gas phase in the chlorination reaction upwards enters the reflux exchanger 1 on reactor top, acetic acid and Acetyl Chloride 98Min. condensation are got off, return reactor, non-condensable gas hydrogenchloride is separated from condenser, and little acetic acid that hydrogenchloride is carried secretly and Acetyl Chloride 98Min. condense on the wall of the electrostatic precipitator on reflux exchanger top and return in the still.After acetic acid reaction finishes in the reactor, stop to annotate chlorine, close microwave generator.Change feed liquid in the still in distiller underpressure distillation, reclaim the Acetyl Chloride 98Min. that steams and use in order to next time, the liquid after the underpressure distillation is the chloroacetic acid solution of purity＞99.5%.This liquid is directly packed in inner lining plastic bag bag weaved, be placed on the vibrations crystallizer, spontaneous nucleation is about 6 hours under vibrating state, is finished product Mono Chloro Acetic Acid crystal.Analytical results shows that dichloroacetic acid content conforms to quality requirements less than 0.5%, and other quality index also conforms to quality requirements.
Claims (8)
1, a kind of method of production of chloroacetic acid, process is: add acetic acid and the aceticanhydride that is equivalent to acetic acid 10～15% in reactor (3), be warming up to 80～100 ℃ and maintenance temperature, normal pressure, feed chlorine and carry out chlorination reaction, carry out product separation after reaction finishes, it is characterized in that: described chlorination reaction is carried out under the microwave power-assisted, and the wavelength of described microwave is 5～20cm.
2, according to the method for the described production of chloroacetic acid of claim 1, it is characterized in that: described product separation is the method for underpressure distillation, and Acetyl Chloride 98Min. of telling and Mono Chloro Acetic Acid liquid are with the chloroacetic acid solution flexible container of packing into, be placed on the vibrations crystallizer spontaneous nucleation under vibrating state.
3, according to the method for the described production of chloroacetic acid of claim 2, it is characterized in that: described flexible container is the woven bag of inner lining plastic bag.
4, a kind of conversion unit of realizing the described production of chloroacetic acid method of claim 1, comprise the reactor (3) of being with glass lining, reflux exchanger (1), be provided with chlorine tube (2) in the reactor, the reactor skin is provided with temperature control chuck (4), it is characterized in that: a microwave generator (6) is installed at described reactor end opening place, and the emitting head of described microwave generator sees through the reactant of the polyfluortetraethylene plate orientating reaction still inside of reactor bottom.
5, conversion unit according to claim 4 is characterized in that: described chlorine tube (2) is a Glass tubing, and the bottom of Glass tubing is with reinforced pipe (7).
6, according to claim 4 or 5 described conversion units, it is characterized in that: director (5) is housed in the described reactor, the structure of described director is: with the concentric two of chlorine tube (2) open tubes, be installed in the bottom of chlorine tube, the emission port of microwave generator is aimed at the end opening of director (5).
7, conversion unit according to claim 6 is characterized in that: described two open tubes is a glass round tube.
8, conversion unit according to claim 4 is characterized in that: electrostatic precipitator is equipped with on the top of described reflux exchanger (1).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200910074525 CN101575281B (en) | 2009-06-24 | 2009-06-24 | Chloroacetic acid producing method and reaction equipment thereof |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200910074525 CN101575281B (en) | 2009-06-24 | 2009-06-24 | Chloroacetic acid producing method and reaction equipment thereof |
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| CN101575281A true CN101575281A (en) | 2009-11-11 |
| CN101575281B CN101575281B (en) | 2013-05-29 |
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| CN 200910074525 Expired - Fee Related CN101575281B (en) | 2009-06-24 | 2009-06-24 | Chloroacetic acid producing method and reaction equipment thereof |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101844058A (en) * | 2010-06-03 | 2010-09-29 | 濮阳市普天化工有限公司 | Equipment for producing chloroacetic acid |
| CN104673388A (en) * | 2013-11-28 | 2015-06-03 | 大连隆星新材料有限公司 | Chlorinated paraffin device |
| CN105949051A (en) * | 2016-05-23 | 2016-09-21 | 河南红东方化工股份有限公司 | Crystalizing process of chloroacetic acid |
| CN107159063A (en) * | 2017-07-12 | 2017-09-15 | 盐城国众化工有限公司 | A kind of chloroacetic preparative separation tower apparatus |
| CN109529798A (en) * | 2018-11-26 | 2019-03-29 | 上海建安化工设计有限公司 | One kind preparing chloroacetic catalyst and its preparation and application for being catalyzed acetic acid |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1096288A (en) * | 1994-02-03 | 1994-12-14 | 太原工业大学 | The chloroacetic production technique of high purity |
| CN1298860A (en) * | 1999-12-08 | 2001-06-13 | 重庆嘉陵化学制品有限公司 | Process for preparing chloracetic acid by continuous chlorination and its equipment |
| CN1566063A (en) * | 2003-07-05 | 2005-01-19 | 山东新华东风化工有限公司 | Production process for chloroacetic acid |
| CN101134722A (en) * | 2007-10-09 | 2008-03-05 | 江苏索普（集团）有限公司 | Method for synthesizing chloroacetic acid |
-
2009
- 2009-06-24 CN CN 200910074525 patent/CN101575281B/en not_active Expired - Fee Related
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1096288A (en) * | 1994-02-03 | 1994-12-14 | 太原工业大学 | The chloroacetic production technique of high purity |
| CN1298860A (en) * | 1999-12-08 | 2001-06-13 | 重庆嘉陵化学制品有限公司 | Process for preparing chloracetic acid by continuous chlorination and its equipment |
| CN1566063A (en) * | 2003-07-05 | 2005-01-19 | 山东新华东风化工有限公司 | Production process for chloroacetic acid |
| CN101134722A (en) * | 2007-10-09 | 2008-03-05 | 江苏索普（集团）有限公司 | Method for synthesizing chloroacetic acid |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101844058A (en) * | 2010-06-03 | 2010-09-29 | 濮阳市普天化工有限公司 | Equipment for producing chloroacetic acid |
| CN104673388A (en) * | 2013-11-28 | 2015-06-03 | 大连隆星新材料有限公司 | Chlorinated paraffin device |
| CN105949051A (en) * | 2016-05-23 | 2016-09-21 | 河南红东方化工股份有限公司 | Crystalizing process of chloroacetic acid |
| CN107159063A (en) * | 2017-07-12 | 2017-09-15 | 盐城国众化工有限公司 | A kind of chloroacetic preparative separation tower apparatus |
| CN109529798A (en) * | 2018-11-26 | 2019-03-29 | 上海建安化工设计有限公司 | One kind preparing chloroacetic catalyst and its preparation and application for being catalyzed acetic acid |
| CN109529798B (en) * | 2018-11-26 | 2021-12-07 | 上海市安装工程集团有限公司 | Catalyst for catalyzing acetic acid to prepare chloroacetic acid, and preparation and application thereof |
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| CN101575281B (en) | 2013-05-29 |
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Granted publication date: 20130529 |