CN105348085A - Continuous preparation technology of m-methyl benzoyl chloride - Google Patents
Continuous preparation technology of m-methyl benzoyl chloride Download PDFInfo
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- CN105348085A CN105348085A CN201510932461.7A CN201510932461A CN105348085A CN 105348085 A CN105348085 A CN 105348085A CN 201510932461 A CN201510932461 A CN 201510932461A CN 105348085 A CN105348085 A CN 105348085A
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- methyl benzoyl
- methyl
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- formyl chloride
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/58—Preparation of carboxylic acid halides
- C07C51/60—Preparation of carboxylic acid halides by conversion of carboxylic acids or their anhydrides or esters, lactones, salts into halides with the same carboxylic acid part
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/42—Separation; Purification; Stabilisation; Use of additives
- C07C51/43—Separation; Purification; Stabilisation; Use of additives by change of the physical state, e.g. crystallisation
- C07C51/44—Separation; Purification; Stabilisation; Use of additives by change of the physical state, e.g. crystallisation by distillation
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- Organic Chemistry (AREA)
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- Oil, Petroleum & Natural Gas (AREA)
- Crystallography & Structural Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention relates to a continuous preparation technology of m-methyl benzoyl chloride, and belongs to the technical field of fine chemical engineering. The continuous preparation technology comprises the steps of adding m-methyl benzoic acid, thionyl chloride and an organic solvent in a reaction kettle for reaction under a condition that a phase transfer catalyst exists, and obtaining reaction liquid; then adding the reaction liquid in a rectifying tower for carrying out normal-pressure rectifying so as to recycle the thionyl chloride and the organic solvent in the reaction liquid, and obtaining a m-methyl benzoyl chloride crude product; adding the m-methyl benzoyl chloride crude product in a film evaporator to carry out pressure-reduction distillation, and obtaining the m-methyl benzoyl chloride. According to the continuous preparation technology disclosed by the invention, the problems existing in a batch method/technology that the product quality is unstable, the automation degree of a device is low, and the labor intensity is large are solved; the continuous preparation technology has the characteristics that the technological route is concise, the production period is short, and the product yield is high; a side reaction can be prevented from being generated while the production capacity is increased.
Description
Technical field
The present invention relates to a kind of continuous production processes of m-methyl benzoyl formyl chloride, belong to technical field of fine.
Background technology
Along with the fast development of macromolecular material, m-methyl benzoyl formyl chloride becomes a kind of important chemical intermediate gradually, more and more receive the concern of numerous researchists, the performance of its excellence obtains and is widely used in medicine, agricultural chemicals, dyestuff and sensitive materials production etc.Batch production technique is mostly adopted to prepare methyl benzoyl chloride at present, batch technology has the advantages that equipment is simple, versatility is wide, when demand is lower, adopt this method comparatively economical, but along with production-scale expansion, adopt batch technology when producing m-methyl benzoyl formyl chloride, there is the problems such as the low and labour intensity of different batches unstable product quality, automation degree of equipment is large.
Summary of the invention
The object of this invention is to provide a kind of continuous production processes of m-methyl benzoyl formyl chloride, have the advantages that operational path is succinct, with short production cycle, product yield is high.
The continuous production processes of m-methyl benzoyl formyl chloride of the present invention, under phase-transfer catalyst existence condition, m-methyl benzoic acid, sulfur oxychloride and organic solvent are joined in reactor and reacts, obtain reaction solution, then reaction solution is joined in rectifying tower and carry out atmospheric distillation to reclaim sulfur oxychloride wherein and organic solvent, obtain m-methyl benzoyl formyl chloride crude product, will join in thin-film evaporator methyl benzoyl chloride crude product and carry out underpressure distillation, and obtain methyl benzoyl chloride.
Wherein:
Described phase-transfer catalyst be tertiary amine and have in the quaternary ammonium salt of ion pair any one or multiple, wherein, the quaternary ammonium salt with ion pair is benzyltriethylammoinium chloride, Tetrabutyl amonium bromide, tetrabutylammonium chloride, 4-butyl ammonium hydrogen sulfate, tri-n-octyl methyl ammonium chloride, Dodecyl trimethyl ammonium chloride and tetradecyl trimethyl ammonium chloride; Tertiary amine is Tributylamine and pyridine.
Described organic solvent is one or more in trichloromethane, ethylene dichloride, dimethylbenzene, ethyl acetate, toluene, methylene dichloride, tetrahydrofuran (THF), benzene, dichlorobenzene.
Described m-methyl benzoic acid and the mol ratio of sulfur oxychloride are 1:1.06-1.13.
Described phase-transfer catalyst consumption is the 0.05-0.15wt% of m-methyl benzoic acid.
Described temperature of reaction is 30-50 DEG C, and the reaction times is 2-6h, has reacted follow-up continuation of insurance temperature 0.5h.
The temperature of described underpressure distillation is 113-120 DEG C, and the vacuum tightness of underpressure distillation is 510-570mmHg.
The thin-film evaporator used in the present invention has the feature that range of viscosities is wide and turndown ratio is large that heat transfer coefficient is high, evaporation capacity is large, low-temperature evaporation is effective, residence time of material is short, be suitable for, and is progressively promoted and applies in the industries such as chemical industry, light industry, pharmacy, environmental protection and food.
Beneficial effect of the present invention is as follows:
Continuous production processes of the present invention has the advantages that operational path is succinct, with short production cycle, product yield is high, and while raising throughput, turn avoid the generation of side reaction, product yield is 97-98%.
Embodiment
Below in conjunction with embodiment, the present invention is described further.
Embodiment 1
The continuous production processes of m-methyl benzoyl formyl chloride is as follows:
(1) 500kg m-methyl benzoic acid, 463kg sulfur oxychloride and 1000kg dimethylbenzene are joined in reactor, then add 0.25kg benzyltriethylammoinium chloride, at 50 DEG C, react 2h, until emerge without gas, continue insulation 0.5h again, obtain reaction solution;
(2) reaction solution is joined in rectifying tower, entering tower flow rate is 4.7kg/min, and the tower reactor of rectifying tower adopts steam heating, and temperature controls at 95 DEG C, the extraction flow of tower top light constituent is 4.2kg/min, and light constituent is back in reactor after condenser condenses;
(3) the m-methyl benzoyl formyl chloride crude product of tower bottom of rectifying tower is joined in thin-film evaporator, feed rate is 3.9kg/min, adjustment vacuum tightness is 510mmHg, underpressure distillation is carried out at 120 DEG C, obtain 551kg m-methyl benzoyl formyl chloride, yield is 97.05%, after testing, and the chromatographic content 99.2% of m-methyl benzoyl formyl chloride.
Embodiment 2
The continuous production processes of m-methyl benzoyl formyl chloride is as follows:
(1) 957kg m-methyl benzoic acid, 919.6kg sulfur oxychloride and 1914kg methylene dichloride are joined in reactor, then add 0.957kg Dodecyl trimethyl ammonium chloride, at 40 DEG C, react 4.5h, until emerge without gas, continue insulation again 0.5 hour, obtain reaction solution;
(2) reaction solution is joined in rectifying tower, entering tower flow rate is 4.7kg/min, and the tower reactor of rectifying tower adopts steam heating, and temperature controls at 99 DEG C, the extraction flow of tower top light constituent is 4.2kg/min, and light constituent is back in reactor after condenser condenses;
(3) the m-methyl benzoyl formyl chloride crude product of tower bottom of rectifying tower is joined in thin-film evaporator, feed rate is 3.9kg/min, adjustment vacuum tightness is 570mmHg, underpressure distillation is carried out at 113 DEG C, obtain 1057kg m-methyl benzoyl formyl chloride, yield is 97.3%, after testing, and the chromatographic content 99.5% of m-methyl benzoyl formyl chloride.
Embodiment 3
The continuous production processes of m-methyl benzoyl formyl chloride is as follows:
(1) 1360kg m-methyl benzoic acid, 1453kg sulfur oxychloride and 2720kg dimethylbenzene are joined in reactor, then add 2.04kg 4-butyl ammonium hydrogen sulfate, at 45 DEG C, react 4h, until emerge without gas, continue insulation again 0.5 hour, obtain reaction solution;
(2) reaction solution is joined in rectifying tower, entering tower flow rate is 4.7kg/min, and the tower reactor of rectifying tower adopts steam heating, and temperature controls at 105 DEG C, the extraction flow of tower top light constituent is 4.2kg/min, and light constituent is back in reactor after condenser condenses;
(3) the m-methyl benzoyl formyl chloride crude product of tower bottom of rectifying tower is joined in thin-film evaporator, feed rate is 3.9kg/min, adjustment vacuum tightness is 630mmHg, underpressure distillation is carried out at 127 DEG C, obtain 1516.5kg m-methyl benzoyl formyl chloride, yield is 98.2%, after testing, and the chromatographic content 99.4% of m-methyl benzoyl formyl chloride.
Claims (10)
1. the continuous production processes of a m-methyl benzoyl formyl chloride, it is characterized in that: under phase-transfer catalyst existence condition, m-methyl benzoic acid, sulfur oxychloride and organic solvent are joined in reactor and reacts, obtain reaction solution, then reaction solution is joined in rectifying tower and carry out atmospheric distillation to reclaim sulfur oxychloride wherein and organic solvent, obtain m-methyl benzoyl formyl chloride crude product, to join in thin-film evaporator methyl benzoyl chloride crude product and carry out underpressure distillation, obtain methyl benzoyl chloride;
Described phase-transfer catalyst be tertiary amine and have in the quaternary ammonium salt of ion pair any one or multiple.
2. the continuous production processes of m-methyl benzoyl formyl chloride according to claim 1, is characterized in that: the mol ratio of m-methyl benzoic acid and sulfur oxychloride is 1:1.06-1.13.
3. the continuous production processes of m-methyl benzoyl formyl chloride according to claim 1, is characterized in that: phase-transfer catalyst consumption is the 0.05-0.15wt% of m-methyl benzoic acid.
4. the continuous production processes of m-methyl benzoyl formyl chloride according to claim 1, is characterized in that: the quaternary ammonium salt with ion pair is benzyltriethylammoinium chloride, Tetrabutyl amonium bromide, tetrabutylammonium chloride, 4-butyl ammonium hydrogen sulfate, tri-n-octyl methyl ammonium chloride, Dodecyl trimethyl ammonium chloride and tetradecyl trimethyl ammonium chloride.
5. the continuous production processes of m-methyl benzoyl formyl chloride according to claim 1, is characterized in that: tertiary amine is Tributylamine and pyridine.
6. the continuous production processes of m-methyl benzoyl formyl chloride according to claim 1, is characterized in that: organic solvent is one or more in trichloromethane, ethylene dichloride, dimethylbenzene, ethyl acetate, toluene, methylene dichloride, tetrahydrofuran (THF), benzene, dichlorobenzene.
7. the continuous production processes of m-methyl benzoyl formyl chloride according to claim 1, is characterized in that: temperature of reaction is 30-50 DEG C, and the reaction times is 2-6h.
8. the continuous production processes of m-methyl benzoyl formyl chloride according to claim 1, is characterized in that: reacted follow-up continuation of insurance temperature 0.5h.
9. the continuous production processes of m-methyl benzoyl formyl chloride according to claim 1, is characterized in that: the temperature of underpressure distillation is 113-120 DEG C.
10. the continuous production processes of m-methyl benzoyl formyl chloride according to claim 1, is characterized in that: the vacuum tightness of underpressure distillation is 510-570mmHg.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201510932461.7A CN105348085A (en) | 2015-12-14 | 2015-12-14 | Continuous preparation technology of m-methyl benzoyl chloride |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110790732A (en) * | 2019-11-19 | 2020-02-14 | 安徽金禾实业股份有限公司 | Furfuryl alcohol refining and purifying method in maltol production |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104230703A (en) * | 2014-09-30 | 2014-12-24 | 烟台裕祥精细化工有限公司 | Method for synthesizing high-purity benzoyl chloride |
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- 2015-12-14 CN CN201510932461.7A patent/CN105348085A/en active Pending
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104230703A (en) * | 2014-09-30 | 2014-12-24 | 烟台裕祥精细化工有限公司 | Method for synthesizing high-purity benzoyl chloride |
Non-Patent Citations (1)
| Title |
|---|
| 郑飞浪等: "苯基呋喃-2-甲酮类化合物的合成及其抑制血管平滑肌细胞（VSMC）增殖活性", 《中国药物化学杂志》 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110790732A (en) * | 2019-11-19 | 2020-02-14 | 安徽金禾实业股份有限公司 | Furfuryl alcohol refining and purifying method in maltol production |
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