CN105949060A - Phenyl chloroformate production technique - Google Patents
Phenyl chloroformate production technique Download PDFInfo
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- CN105949060A CN105949060A CN201610384248.1A CN201610384248A CN105949060A CN 105949060 A CN105949060 A CN 105949060A CN 201610384248 A CN201610384248 A CN 201610384248A CN 105949060 A CN105949060 A CN 105949060A
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- agitator tank
- tank
- phenyl chloroformate
- phosgene
- phenol
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C68/00—Preparation of esters of carbonic or haloformic acids
- C07C68/02—Preparation of esters of carbonic or haloformic acids from phosgene or haloformates
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- Organic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Polyesters Or Polycarbonates (AREA)
Abstract
The invention provides a phenyl chloroformate production technique. The technique comprises the steps of firstly, slowly increasing the temperature of a stirring tank, then introducing phosgene constantly into the stirring tank from the middle of the side wall of the stirring tank, opening a phenol dropwise adding tank, and opening the stirring tank and a catalyst spray tank at the same time; secondly, continuing to introduce phosgene, and taking a central control sample; thirdly, continuously extracting the central control sample every other 30 min; fourthly, conducting air expelling with nitrogen on the stirring tank after final sampling is stopped; finally, conducting reduced pressure distillation on materials left after air expelling to obtain phenyl chloroformate. Compared with the prior art, the production technique has the advantages that reaction time is shortened, and purity and reaction efficiency are improved.
Description
Technical field
The present invention relates to field of fine chemical, be specifically related to the production technology of a kind of phenyl chloroformate.
Background technology
Phenyl chloroformate is a kind of important fine-chemical intermediate, has extensive use in terms of chemical industry synthesis, permissible
As polymerization catalyst, plastic modifier, fibre finish, and medicine, the intermediate of pesticide.
The primary synthetic methods of phenyl chloroformate is phosgenation, is dissolved in by phenol under chloroform, cooling and is passed through phosgene, makes absorption
The amount ratio of the material such as light tolerance and phenol, in the amount DMA of the materials such as the 5-10 DEG C of lower dropping of stirring.Then add
Cold water dilutes, and divides and takes oil reservoir, successively with dilute hydrochloric acid and water washing.Dried through anhydrous calcium chloride, Distillation recovery chloroform, then reduce pressure
Rectification, collects 74-75 DEG C of (1.73kPa) fraction, is phenyl chloroformate, yield about 90%.The method post processing is complicated, needs
Reclaiming substantial amounts of solvent, the wastewater flow rate of generation is more, and uses substantial amounts of DMA to do acid binding agent, production cost
High.
The existing production technology disclosing a kind of solventless method phenyl chloroformate, directly adds a small amount of catalysis by melted phenol
Agent, high temperature leads to light, then obtains the content phenyl chloroformate more than 98% by rectification under vacuum, and the method post processing is simple, it is to avoid
A large amount of acid binding agents and the use of solvent, produce without technique waste water, and cost is relatively low, is suitable for industrialized production.
But existing technology there is also by-product production, production efficiency also ratio is relatively low simultaneously, benzene the most in process of production
Phenol can produce by-product diphenyl carbonate (DPC) with product phenyl chloroformate, i.e. under conditions of high temperature and acid binding agent
Summary of the invention
For above problems of the prior art, the invention provides the production technology of a kind of phenyl chloroformate, subtract
Lack the generation of by-product, improve production efficiency.
The present invention is achieved by the following technical solutions:
A kind of production technology of phenyl chloroformate, its production method comprises the following steps:
1) temperature of agitator tank is slowly raised 97-102 DEG C, then to logical in agitator tank in the middle part of the sidewall of agitator tank
Enter phosgene, and the intake of phosgene is 50-60mol, and be continually fed into phosgene, be then turned on phenol dropping tank, open simultaneously
Stirring and open catalyst sprayed tank, and speed 70-140L/h of dropping phenol, the response time is 2 little to take middle control sample constantly,
Gas phase normalizing analyzes the area percentage of phenyl chloroformate and Main By product diphenyl carbonate；
2) being continually fed into phosgene again, the speed of dropping phenol is 30-35L/h, and the response time is 4 little to take middle control sample constantly,
Gas phase normalizing analyzes the area percentage of phenyl chloroformate and Main By product diphenyl carbonate；
3) continue above-mentioned middle control sample 30 minutes to extract once so that above-mentioned continuation is reacted to phenyl chloroformate and main pair
The area percentage of product diphenyl carbonate is not further added by, and sampling number of times is 10-12 time；
4), after the agitator tank after aforementioned final sampling being stopped uses nitrogen to catch up with gas, by tail gas by condenser, isolate
Organic solvent so that the content of organic solvent is at 5-8ppm, then tail gas is passed through phosgene decomposition absorption tower,；
5) by aforementioned catch up with gas after material use decompression distill out phenyl chloroformate.
Further, phenol dropping tank is set in the oblique upper of agitator tank, catalyst spray is set in the side of agitator tank
Tank, and the liquid outlet connection drain pipe of catalyst sprayed tank low side, the liquid outlet of drain pipe arranges shower nozzle, catalyst sprayed tank
Shower nozzle is arranged on the middle part of agitator tank inwall, and shower nozzle is towards the middle and upper part of agitator tank.
Further, the middle part of agitator tank arranges phosgene air inlet, and agitator tank side connects circulating refrigerator, agitator tank
Outside arranges chuck, and the outer wall of institute's agitator tank arranges temperature control zone road, and temperature control zone road is connected with described circulating refrigerator,
Temperature controls temperature control zone road and is positioned at the chuck of described agitator tank, and the gas outlet on agitator tank top connects condenser, agitator tank
Top plugs and is equipped with thermometer.
Further, wherein the mass ratio of catalyst and described phenol is 1-1.2:20.
Further, catalyst is DMAP or three grades of organic amines.
The invention have the benefit that the present invention's compares existing production technology, owing to using anhydrous response thing phenol
The mode of dropping, and phosgene reaction, under catalyst with certain temperature conditions so that the response time is little by existing 7-12
Time, shorten to 4-10 hour, quickly and completely react with phosgene owing to dropwise reaction enables to reactant phenol, can avoid
The generation of by-product diphenyl carbonate, therefore further increases the purity of product phenyl chloroformate, and purity can reach
98.9-99.4%, and this reaction is also easy to control, and the most on the whole, shortens the time of reaction, improves purity and anti-
Answer efficiency.
Detailed description of the invention
In order to make the purpose of the present invention, technical scheme and advantage clearer, below in conjunction with embodiment, to the present invention
It is further elaborated.Should be appreciated that specific embodiment described herein, only in order to explain the present invention, is not used to
Limit the present invention.
Embodiment 1
First, the temperature of agitator tank is slowly raised 100 DEG C, then to logical in agitator tank in the middle part of the sidewall of agitator tank
Enter phosgene, and the intake of phosgene is 60mol, and be continually fed into phosgene, be then turned on phenol dropping tank, open stirring simultaneously
With open catalyst sprayed tank, and dropping phenol speed 70-140L/h, the response time be 2 little constantly, take middle control sample, gas phase
Normalizing analyzes the area percentage of phenyl chloroformate and Main By product diphenyl carbonate；
Secondly, then being continually fed into phosgene, the speed of dropping phenol is 30L/h, and the response time is 4 little to take middle control sample constantly,
Gas phase normalizing analyzes the area percentage of phenyl chloroformate and Main By product diphenyl carbonate；
Again, continue above-mentioned middle control sample 30 minutes to extract once so that above-mentioned continuation is reacted to phenyl chloroformate and master
The area percentage wanting by-product diphenyl carbonate is not further added by, and sampling number of times is 10 times；
Then, after the agitator tank after aforementioned final sampling being stopped uses nitrogen to catch up with gas, by tail gas by condenser, separate
Go out organic solvent so that the content of organic solvent is at 8ppm, then tail gas is passed through phosgene decomposition absorption tower,；Finally, by front
Stating the material after catching up with gas uses decompression to distill out phenyl chloroformate.
Specifically, phenol dropping tank is set in the oblique upper of agitator tank, catalyst sprayed tank is set in the side of agitator tank,
And the liquid outlet of catalyst sprayed tank low side connects drain pipe, the liquid outlet of drain pipe arranges shower nozzle, the spray of catalyst sprayed tank
Head is arranged on the middle part of agitator tank inwall, and shower nozzle is towards the middle and upper part of agitator tank.
Specifically, the middle part of agitator tank arranges phosgene air inlet, and agitator tank side connects circulating refrigerator, outside agitator tank
Side arranges chuck, and the outer wall of institute's agitator tank arranges temperature control zone road, and temperature control zone road is connected with described circulating refrigerator, temperature
Degree controls temperature control zone road and is positioned at the chuck of described agitator tank, and the gas outlet on agitator tank top connects condenser, stirs tank deck
End plugs and is equipped with thermometer.Wherein catalyst is 1:20 with the mass ratio of described phenol；Catalyst is three grades of organic amines.
The present invention compares existing production technology, owing to using the mode of anhydrous response thing phenol dropping, anti-with phosgene
Should, under catalyst with certain temperature conditions so that the response time, by existing 7-12 hour, shortens to 4-10 hour, by
Enable to reactant phenol in dropwise reaction quickly and completely react with phosgene, can be avoided by-product diphenyl carbonate
Produce, therefore further increase the purity of product phenyl chloroformate, and purity can reach 98.9%, and this reaction is the easiest
In control, the most on the whole, shorten the time of reaction, improve purity and reaction efficiency.
Embodiment 2
First, the temperature of agitator tank is slowly raised 99 DEG C, then to logical in agitator tank in the middle part of the sidewall of agitator tank
Enter phosgene, and the intake of phosgene is 50mol, and be continually fed into phosgene, be then turned on phenol dropping tank, open stirring simultaneously
With open catalyst sprayed tank, and dropping phenol speed 70-140L/h, the response time be 2 little constantly, take middle control sample, gas phase
Normalizing analyzes the area percentage of phenyl chloroformate and Main By product diphenyl carbonate；
Secondly, then being continually fed into phosgene, the speed of dropping phenol is 31L/h, and the response time is 4 little to take middle control sample constantly,
Gas phase normalizing analyzes the area percentage of phenyl chloroformate and Main By product diphenyl carbonate；
Again, continue above-mentioned middle control sample 30 minutes to extract once so that above-mentioned continuation is reacted to phenyl chloroformate and master
The area percentage wanting by-product diphenyl carbonate is not further added by, and sampling number of times is 12 times；
Then, after the agitator tank after aforementioned final sampling being stopped uses nitrogen to catch up with gas, by tail gas by condenser, separate
Go out organic solvent so that the content of organic solvent is at 6ppm, then tail gas is passed through phosgene decomposition absorption tower,；Finally, by front
Stating the material after catching up with gas uses decompression to distill out phenyl chloroformate.
Specifically, phenol dropping tank is set in the oblique upper of agitator tank, catalyst sprayed tank is set in the side of agitator tank,
And the liquid outlet of catalyst sprayed tank low side connects drain pipe, the liquid outlet of drain pipe arranges shower nozzle, the spray of catalyst sprayed tank
Head is arranged on the middle part of agitator tank inwall, and shower nozzle is towards the middle and upper part of agitator tank.
Specifically, the middle part of agitator tank arranges phosgene air inlet, and agitator tank side connects circulating refrigerator, outside agitator tank
Side arranges chuck, and the outer wall of institute's agitator tank arranges temperature control zone road, and temperature control zone road is connected with described circulating refrigerator, temperature
Degree controls temperature control zone road and is positioned at the chuck of described agitator tank, and the gas outlet on agitator tank top connects condenser, stirs tank deck
End plugs and is equipped with thermometer.
Wherein catalyst is 1:20 with the mass ratio of described phenol；Catalyst is DMAP.
The present invention compares existing production technology, owing to using the mode of anhydrous response thing phenol dropping, anti-with phosgene
Should, under catalyst with certain temperature conditions so that the response time, by existing 7-12 hour, shortens to 4-10 hour, by
Enable to reactant phenol in dropwise reaction quickly and completely react with phosgene, can be avoided by-product diphenyl carbonate
Produce, therefore further increase the purity of product phenyl chloroformate, and purity can reach 99%, and this reaction is also easy to
Control, the most on the whole, shorten the time of reaction, improve purity and reaction efficiency
Embodiment 3
First, the temperature of agitator tank is slowly raised 101 DEG C, then to logical in agitator tank in the middle part of the sidewall of agitator tank
Enter phosgene, and the intake of phosgene is 50mol, and be continually fed into phosgene, be then turned on phenol dropping tank, open stirring simultaneously
With open catalyst sprayed tank, and dropping phenol speed 70L/h, the response time be 2 little constantly, take middle control sample, gas phase normalizing
Analyze the area percentage of phenyl chloroformate and Main By product diphenyl carbonate；
Secondly, then being continually fed into phosgene, the speed of dropping phenol is 32L/h, and the response time is 4 little to take middle control sample constantly,
Gas phase normalizing analyzes the area percentage of phenyl chloroformate and Main By product diphenyl carbonate；
Again, continue above-mentioned middle control sample 30 minutes to extract once so that above-mentioned continuation is reacted to phenyl chloroformate and master
The area percentage wanting by-product diphenyl carbonate is not further added by, and sampling number of times is 10 times；
Then, after the agitator tank after aforementioned final sampling being stopped uses nitrogen to catch up with gas, by tail gas by condenser, separate
Go out organic solvent so that the content of organic solvent is at 5ppm, then tail gas is passed through phosgene decomposition absorption tower,；Finally, by front
Stating the material after catching up with gas uses decompression to distill out phenyl chloroformate.
Specifically, phenol dropping tank is set in the oblique upper of agitator tank, catalyst sprayed tank is set in the side of agitator tank,
And the liquid outlet of catalyst sprayed tank low side connects drain pipe, the liquid outlet of drain pipe arranges shower nozzle, the spray of catalyst sprayed tank
Head is arranged on the middle part of agitator tank inwall, and shower nozzle is towards the middle and upper part of agitator tank.
Specifically, the middle part of agitator tank arranges phosgene air inlet, and agitator tank side connects circulating refrigerator, outside agitator tank
Side arranges chuck, and the outer wall of institute's agitator tank arranges temperature control zone road, and temperature control zone road is connected with described circulating refrigerator, temperature
Degree controls temperature control zone road and is positioned at the chuck of described agitator tank, and the gas outlet on agitator tank top connects condenser, stirs tank deck
End plugs and is equipped with thermometer.
Wherein catalyst is 1:20 with the mass ratio of described phenol；Catalyst is three grades of organic amines.
The present invention compares existing production technology, owing to using the mode of anhydrous response thing phenol dropping, anti-with phosgene
Should, under catalyst with certain temperature conditions so that the response time, by existing 7-12 hour, shortens to 4-10 hour, by
Enable to reactant phenol in dropwise reaction quickly and completely react with phosgene, can be avoided by-product diphenyl carbonate
Produce, therefore further increase the purity of product phenyl chloroformate, and purity can reach 99.1%, and this reaction is the easiest
In control, the most on the whole, shorten the time of reaction, improve purity and reaction efficiency.
Embodiment 4
First, the temperature of agitator tank is slowly raised 97 DEG C, then to logical in agitator tank in the middle part of the sidewall of agitator tank
Enter phosgene, and the intake of phosgene is 58mol, and be continually fed into phosgene, be then turned on phenol dropping tank, open stirring simultaneously
With open catalyst sprayed tank, and dropping phenol speed 120L/h, the response time be 2 little constantly, take middle control sample, gas phase normalizing
Analyze the area percentage of phenyl chloroformate and Main By product diphenyl carbonate；
Secondly, then being continually fed into phosgene, the speed of dropping phenol is 34L/h, and the response time is 4 little to take middle control sample constantly,
Gas phase normalizing analyzes the area percentage of phenyl chloroformate and Main By product diphenyl carbonate；
Again, continue above-mentioned middle control sample 30 minutes to extract once so that above-mentioned continuation is reacted to phenyl chloroformate and master
The area percentage wanting by-product diphenyl carbonate is not further added by, and sampling number of times is 11 times；
Then, after the agitator tank after aforementioned final sampling being stopped uses nitrogen to catch up with gas, by tail gas by condenser, separate
Go out organic solvent so that the content of organic solvent is at 7ppm, then tail gas is passed through phosgene decomposition absorption tower,；Finally, by front
Stating the material after catching up with gas uses decompression to distill out phenyl chloroformate.
Specifically, phenol dropping tank is set in the oblique upper of agitator tank, catalyst sprayed tank is set in the side of agitator tank,
And the liquid outlet of catalyst sprayed tank low side connects drain pipe, the liquid outlet of drain pipe arranges shower nozzle, the spray of catalyst sprayed tank
Head is arranged on the middle part of agitator tank inwall, and shower nozzle is towards the middle and upper part of agitator tank.
Specifically, the middle part of agitator tank arranges phosgene air inlet, and agitator tank side connects circulating refrigerator, outside agitator tank
Side arranges chuck, and the outer wall of institute's agitator tank arranges temperature control zone road, and temperature control zone road is connected with described circulating refrigerator, temperature
Degree controls temperature control zone road and is positioned at the chuck of described agitator tank, and the gas outlet on agitator tank top connects condenser, stirs tank deck
End plugs and is equipped with thermometer.
Wherein catalyst is 1:20 with the mass ratio of described phenol；Catalyst is DMAP.
The present invention compares existing production technology, owing to using the mode of anhydrous response thing phenol dropping, anti-with phosgene
Should, under catalyst with certain temperature conditions so that the response time, by existing 7-12 hour, shortens to 4-10 hour, by
Enable to reactant phenol in dropwise reaction quickly and completely react with phosgene, can be avoided by-product diphenyl carbonate
Produce, therefore further increase the purity of product phenyl chloroformate, and purity can reach 99.3%, and this reaction is the easiest
In control, the most on the whole, shorten the time of reaction, improve purity and reaction efficiency.
Embodiment 5
First, the temperature of agitator tank is slowly raised 102 DEG C, then to logical in agitator tank in the middle part of the sidewall of agitator tank
Enter phosgene, and the intake of phosgene is 60mol, and be continually fed into phosgene, be then turned on phenol dropping tank, open stirring simultaneously
With open catalyst sprayed tank, and dropping phenol speed 140L/h, the response time be 2 little constantly, take middle control sample, gas phase normalizing
Analyze the area percentage of phenyl chloroformate and Main By product diphenyl carbonate；
Secondly, then being continually fed into phosgene, the speed of dropping phenol is 35L/h, and the response time is 4 little to take middle control sample constantly,
Gas phase normalizing analyzes the area percentage of phenyl chloroformate and Main By product diphenyl carbonate；
Again, continue above-mentioned middle control sample 30 minutes to extract once so that above-mentioned continuation is reacted to phenyl chloroformate and master
The area percentage wanting by-product diphenyl carbonate is not further added by, and sampling number of times is 10 times；
Then, after the agitator tank after aforementioned final sampling being stopped uses nitrogen to catch up with gas, by tail gas by condenser, separate
Go out organic solvent so that the content of organic solvent is at 8ppm, then tail gas is passed through phosgene decomposition absorption tower,；Finally, by front
Stating the material after catching up with gas uses decompression to distill out phenyl chloroformate.
Specifically, phenol dropping tank is set in the oblique upper of agitator tank, catalyst sprayed tank is set in the side of agitator tank,
And the liquid outlet of catalyst sprayed tank low side connects drain pipe, the liquid outlet of drain pipe arranges shower nozzle, the spray of catalyst sprayed tank
Head is arranged on the middle part of agitator tank inwall, and shower nozzle is towards the middle and upper part of agitator tank.
Specifically, the middle part of agitator tank arranges phosgene air inlet, and agitator tank side connects circulating refrigerator, outside agitator tank
Side arranges chuck, and the outer wall of institute's agitator tank arranges temperature control zone road, and temperature control zone road is connected with described circulating refrigerator, temperature
Degree controls temperature control zone road and is positioned at the chuck of described agitator tank, and the gas outlet on agitator tank top connects condenser, stirs tank deck
End plugs and is equipped with thermometer.
Wherein catalyst is 1:20 with the mass ratio of described phenol；Catalyst is DMAP (DMAP).
The present invention compares existing production technology, owing to using the mode of anhydrous response thing phenol dropping, anti-with phosgene
Should, under catalyst with certain temperature conditions so that the response time, by existing 7 hours, shortens to 5 hours, due to dropping
Reaction enables to reactant phenol and quickly and completely reacts with phosgene, can be avoided the generation of by-product diphenyl carbonate,
Therefore further increase the purity of product phenyl chloroformate, and purity can reach 99.4%, and this reaction is also easy to control
System, the most on the whole, shortens the time of reaction, improves purity and reaction efficiency.
The foregoing is only presently preferred embodiments of the present invention, not in order to limit the present invention, all essences in the present invention
Any amendment, equivalent and the improvement etc. made within god and principle, should be included within the scope of the present invention.
Claims (5)
1. the production technology of a phenyl chloroformate, it is characterised in that: its production method comprises the following steps:
1) temperature of agitator tank is slowly raised 97-102 DEG C, then in the middle part of the sidewall of agitator tank, in agitator tank, is passed through light
Gas, and the intake of phosgene is 50-60mol, and it is continually fed into phosgene, it is then turned on phenol dropping tank, opens stirring simultaneously
With open catalyst sprayed tank, and dropping phenol speed 70-140L/h, the response time be 2 little constantly, take middle control sample, gas phase
Normalizing analyzes the area percentage of phenyl chloroformate and Main By product diphenyl carbonate；
2) be continually fed into phosgene again, dropping phenol speed be 30-35L/h, the response time be 4 little constantly, take middle control sample, gas phase
Normalizing analyzes the area percentage of phenyl chloroformate and Main By product diphenyl carbonate；
3) continue above-mentioned middle control sample 30 minutes to extract once so that above-mentioned continuation is reacted to phenyl chloroformate and Main By product
The area percentage of diphenyl carbonate is not further added by, and sampling number of times is 10-12 time；
4), after the agitator tank after aforementioned final sampling being stopped uses nitrogen to catch up with gas, by tail gas by condenser, isolate organic
Solvent so that the content of organic solvent is at 5-8ppm, then tail gas is passed through phosgene decomposition absorption tower,；
5) by aforementioned catch up with gas after material use decompression distill out phenyl chloroformate.
The production technology of a kind of phenyl chloroformate the most according to claim 1, it is characterised in that: in the oblique upper of agitator tank
Phenol dropping tank is set, catalyst sprayed tank is set in the side of agitator tank, and the liquid outlet of catalyst sprayed tank low side connects
Drain pipe, the liquid outlet of drain pipe arranges shower nozzle, and the shower nozzle of catalyst sprayed tank is arranged on the middle part of agitator tank inwall, and shower nozzle
Middle and upper part towards agitator tank.
The production technology of a kind of phenyl chloroformate the most according to claim 1, it is characterised in that: the middle part of agitator tank is arranged
Phosgene air inlet, agitator tank side connects circulating refrigerator, and the outside of agitator tank arranges chuck, and the outer wall of institute's agitator tank arranges temperature
Degree controls pipeline, and temperature control zone road is connected with described circulating refrigerator, and temperature controls temperature control zone road and is positioned at described stirring
The chuck of tank, the gas outlet on agitator tank top connects condenser, and agitator tank top plugs and is equipped with thermometer.
The production technology of a kind of phenyl chloroformate the most according to claim 1, it is characterised in that: catalyst and described phenol
Mass ratio be 1-1.2:20.
5. according to the production technology of a kind of phenyl chloroformate described in claim 1 or 4, it is characterised in that: catalyst is DMAP
Or three grades of organic amines.
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| CN109621656A (en) * | 2018-12-29 | 2019-04-16 | 安徽广信农化股份有限公司 | A kind of tail gas treatment process synthesizing NSC 87419 |
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| CN109621656A (en) * | 2018-12-29 | 2019-04-16 | 安徽广信农化股份有限公司 | A kind of tail gas treatment process synthesizing NSC 87419 |
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