CN216538433U - Benzophenone serialization production system - Google Patents
Benzophenone serialization production system Download PDFInfo
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- CN216538433U CN216538433U CN202122719094.6U CN202122719094U CN216538433U CN 216538433 U CN216538433 U CN 216538433U CN 202122719094 U CN202122719094 U CN 202122719094U CN 216538433 U CN216538433 U CN 216538433U
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Abstract
The utility model discloses a continuous production system of benzophenone, a neutralization kettle is connected with an alkaline water elevated tank, the neutralization kettle is connected with a neutralization continuous separator, a water phase discharge pipeline and an organic phase discharge pipeline of the neutralization continuous separator are respectively connected with a hydrolysis water storage tank and a primary washing kettle, a water inlet pipe of the primary washing kettle is connected with the primary washing water storage tank, the primary washing kettle is connected with a primary washing separator, a water phase discharge pipeline of the primary washing separator is connected with the neutralization water storage tank and the hydrolysis water storage tank, an organic phase discharge pipeline is connected with a secondary washing kettle, the secondary washing kettle is connected with a secondary washing separator, a water phase discharge pipeline of the secondary washing separator is connected with the primary washing water storage tank, the connection among all levels of equipment through pipelines is realized through reasonable configuration of the equipment, automatic control is realized through an automatic control valve, automatic material addition is realized, and automatic continuous production is realized, the productivity is improved, the labor intensity of workers is reduced, raw materials such as benzene and the like can be better recovered, and the wastewater amount is reduced.
Description
Technical Field
The utility model relates to the field of benzophenone production, in particular to a benzophenone continuous production system.
Background
Benzophenone is an intermediate of ultraviolet absorbers, organic pigments, medicines, perfumes, and insecticides. The compound is used for producing dicyclohexylpiperidine, benztropine hydrobromide, diphenhydramine hydrochloride and the like in the pharmaceutical industry. The natural essence is also a styrene polymerization inhibitor and a spice flavor fixative, can endow the spice with sweet smell, is used in various perfumes and soap flavors, and can be used for preparing edible essences such as almond, peach, cream, coconut and the like.
The phosgene method synthesis process of the benzophenone comprises the following steps: benzene and phosgene are subjected to acylation reaction under the action of Lewis acid aluminum trichloride, and electrophilic groups of benzene rings are subjected to substitution reaction to produce a benzophenone-aluminum trichloride complex. Then the mixture and water are hydrolyzed, and the mixture of benzophenone and benzene and the aluminum trichloride aqueous solution (byproduct) are separated after standing and layering. And (3) treating the unseparated acidic impurities in the materials by the hydrolyzed organic phase through neutralization reaction, separating, washing with water, and washing soluble salts in the materials to achieve the purpose of purifying the organic phase. And (3) sequentially carrying out water-benzene atmospheric distillation on the washed materials to separate most of benzene in the organic phase, and rectifying to obtain the benzophenone.
The existing process can not realize continuous production, thus resulting in low production efficiency and low yield.
Secondly, the existing process can not well recover the washing liquid and the main raw material benzene, which causes large wastewater amount, large benzene consumption and environmental pollution.
Finally, the existing process adopts a one-pot method for rectification, 50% caustic soda solution is added, the front fraction is distilled out firstly, and then the benzophenone product is distilled out. The recovery rate is low and the rate of finished products is low.
SUMMERY OF THE UTILITY MODEL
Aiming at the problems in the prior art, the utility model provides a continuous benzophenone production system, which can realize continuous production after neutralization, improve the production efficiency and the productivity, and can recycle water washing liquid and reduce the amount of wastewater.
In order to achieve the purpose, the utility model is realized by the following technical scheme: the utility model provides a benzophenone serialization production system, is including hydrolysising the stock chest and the neutralization kettle, be provided with agitating unit, its characterized in that in the neutralization kettle: the hydrolysis storage tank is connected with the neutralization kettle through a flowmeter and an automatic control valve, an alkaline water adding pipeline is arranged on the neutralization kettle and is connected with an alkaline water elevated tank, a flowmeter and an automatic control valve are arranged on the alkaline water adding pipeline, a neutralization liquid discharge pipeline is arranged at the bottom of the neutralization kettle and is connected with a neutralization continuous separator, an automatic control valve is arranged on the neutralization liquid discharge pipeline, a water phase discharge pipeline and an organic phase discharge pipeline are arranged on the neutralization continuous separator and are respectively connected with the hydrolysis water storage tank and the primary washing kettle, automatic control valves are respectively arranged on the water phase discharge pipeline and the organic phase discharge pipeline, a water inlet pipe of the primary washing kettle is connected with the primary washing water storage tank through the automatic control valve and the flowmeter, a discharge pipeline is arranged at the bottom of the primary washing kettle and is connected with the primary washing separator, a water phase discharge pipeline and an organic phase discharge pipeline are respectively arranged on the primary washing separator, the water phase discharge pipeline links to each other with the neutralizing water storage tank and the water storage tank of hydrolysising simultaneously to all be provided with automatic control valve, the neutralizing water storage tank links to each other with the neutralizing kettle, organic phase discharge pipeline links to each other with the second grade washing cauldron, all be provided with automatic control valve on the discharge pipeline of the water phase discharge pipeline of one-level washing separator, organic phase discharge pipeline and one-level washing cauldron, the bottom of second grade washing cauldron is provided with washing liquid discharge pipeline and links to each other with the second grade washing separator, the water phase discharge pipeline of second grade washing separator links to each other with the one-level washing water storage tank, the organic phase discharge pipeline of second grade washing separator links to each other with the washing material storage tank, all be provided with automatic control valve on the bottom washing liquid discharge pipeline of the organic phase discharge pipeline of second grade washing separator, water phase discharge pipeline and second grade washing cauldron.
By adopting the scheme, materials at all levels are controlled to be added through the automatic control valve, and the adding amount is controlled through the flow meter, so that automatic continuous production can be realized. The water washing kettle and the separator are separated, and are not separated in the water washing kettle, so that the idle time of the water washing kettle and the separator is reduced, and continuous production is realized. The secondary water washing liquid is used for washing and is applied mechanically, so that the waste water amount is reduced.
In the process, soft water and a neutralized material are forcibly mixed, so that soluble salts such as aluminum salt, sodium salt and the like in the material are dissolved in the water; and then the organic phase and the water phase are subjected to layered continuous separation by utilizing the property of low solubility of the organic phase in water, so that the salt in the organic phase is separated out.
In the scheme, the alkaline water elevated tank is connected with the alkaline water preparation tank through a pipeline, and an automatic control valve and a flowmeter are arranged on the pipeline.
In the above scheme, the washing material storage tank passes through the pipeline and links to each other with washing material pre-heater, is provided with flowmeter and automatic control valve on this pipeline, washing material pre-heater passes through automatic control valve and flowmeter and links to each other with the water benzene distillation column, the water benzene steam pipeline of water benzene distillation column passes through automatic control valve and links to each other with the water benzene condenser, the condensate outlet line of benzene condenser passes through automatic control valve and links to each other with water benzene continuous separation ware, the benzene outlet line of water benzene continuous separation ware passes through automatic control valve and links to each other with the benzene accumulator, the outlet line of benzene accumulator passes through automatic control valve and links to each other with the benzene transfer tank. The water washing material enters a water benzene distillation tower after being preheated, and by utilizing the characteristics of large difference of boiling points and large difference of volatility of components such as water, benzene and benzophenone, the components in the material are partially vaporized and partially condensed for many times in the tower by adopting tower type normal pressure distillation, so that water and most of pure benzene are separated. Thereby recovering benzene.
In the scheme, the tower bottom coarse material outlet pipeline of the water benzene distillation tower is connected with the light component removal tower through an automatic control valve, the benzene and low boiling point gas outlet pipeline of the light component removing tower is connected with the light component removing condenser through an automatic control valve, the liquid outlet pipe of the lightness-removing condenser is connected with the water washing material storage tank through an automatic control valve, the coarse material outlet pipeline of the lightness-removing tower is connected with the rectifying tower through the automatic control valve, the benzophenone steam outlet pipeline of the rectifying tower is connected with a rectifying condenser through an automatic control valve, the rectification condenser is connected with a rectification reflux tank through an automatic control valve, the rectification reflux tank is connected with a reflux port of a rectification tower through a benzophenone reflux pipeline, the benzophenone return line is provided with an automatic control valve and a flowmeter, and the rectification reflux tank is also connected with a benzophenone finished product tank through the automatic control valve. The method comprises two devices of a light component removal tower and a rectification tower, wherein the light component removal tower further separates front fractions, and the rectification tower rectifies the benzophenone without adding a reducing liquid. And returning the front fraction of the light component removal tower to a material washing storage tank.
In the scheme, a raffinate discharge pipeline of the rectifying tower is connected with a raffinate distillation kettle, a steam outlet pipeline of the raffinate distillation kettle is connected with a benzophenone condenser through an automatic control valve, a light fraction outlet of the benzophenone condenser is connected with a light fraction receiving tank through an automatic control valve, and a benzophenone outlet of the benzophenone condenser is connected with the benzophenone receiving tank through an automatic control valve. And further recovering benzophenone and light fraction from the residual liquid of the rectifying tower through a residual liquid distilling still.
In the above scheme, the residue of raffinate stills gets into raffinate hot washing cauldron, the waste water outlet pipeline of raffinate hot washing cauldron passes through automatic control valve and links to each other with raffinate wastewater disposal basin, and waste water decontamination water treatment station, residue shift to incineration disposal.
Has the advantages that: the utility model realizes connection among various levels of equipment through the reasonable configuration of the equipment, realizes automatic control and automatic feeding through the automatic control valve, realizes automatic continuous production, improves the productivity, reduces the labor intensity of workers, can better recover raw materials such as benzene and the like, reduces the waste water amount and realizes green and environment-friendly continuous production.
Drawings
FIG. 1 is a process flow diagram of the present invention.
Detailed Description
The utility model will be further described with reference to the following examples and the accompanying drawings.
Example 1
As shown in figure 1, the continuous benzophenone production system comprises an alkaline water preparation tank 1, an alkaline water elevated tank 2, a hydrolysis material storage tank 3, a neutralization kettle 4, a hydrolysis water storage tank 5, a neutralization continuous separator 6, a primary washing kettle 7, a primary washing water storage tank 8, a primary washing separator 9, a secondary washing kettle 10, a secondary washing separator 11, a washing material storage tank 12, a neutralization water storage tank 13, a washing material preheater 14, a benzene distiller 15, a benzene condenser 16 and a benzene continuous separator 17, a benzene recovery tank 18, a benzene transfer tank 19, a lightness-removing column 20, a lightness-removing condenser 21, a rectifying column 22, a rectifying condenser 23, a rectifying reflux tank 24, a benzophenone finished product tank 25, a raffinate distillation kettle 26, a benzophenone condenser 27, a benzophenone receiving tank 28, a light fraction receiving tank 29, a raffinate hot washing kettle 30, a raffinate waste water tank 31, a pipeline, a pump, an automatic control valve, a flow meter and the like.
A stirring device is arranged in the neutralization kettle 4, the hydrolysis storage tank 3 is connected with the neutralization kettle 4 through a flowmeter, an automatic control valve and a pump, an alkaline water adding pipeline is arranged on the neutralization kettle 4 and connected with the alkaline water elevated tank 2, the flowmeter and the automatic control valve are arranged on the alkaline water adding pipeline, the elevated tank is adopted, and the pump is not needed. The alkaline water high-level tank 2 is connected with the alkaline water preparation tank 1 through a pipeline, and an automatic control valve and a flowmeter are arranged on the pipeline.
The bottom of the neutralization kettle 4 is provided with a neutralization liquid discharge pipeline connected with the neutralization continuous separator 6, the neutralization liquid discharge pipeline is provided with an automatic control valve, the neutralization continuous separator 6 is provided with a water phase discharge pipeline and an organic phase discharge pipeline which are respectively connected with the hydrolysis water storage tank 5 and the first-stage washing kettle 7, the water phase discharge pipeline and the organic phase discharge pipeline are both provided with automatic control valves, the water inlet pipe of the first-stage washing kettle 7 is connected with the first-stage washing water storage tank 8 through the automatic control valves and a flowmeter, the bottom of the first-stage washing kettle 7 is provided with a discharge pipeline connected with the first-stage washing separator 9, the first-stage washing separator 9 is respectively provided with a water phase discharge pipeline and an organic phase discharge pipeline, the water phase discharge pipeline is simultaneously connected with the neutralization water storage tank 13 and the hydrolysis water storage tank 5, and is provided with an automatic control valve. The neutralization water storage tank 13 is connected with the neutralization kettle 4, the organic phase discharge pipeline is connected with the second-stage washing kettle 10, the water phase discharge pipeline of the first-stage washing separator 9, the automatic control valves are arranged on the organic phase discharge pipeline and the discharge pipeline of the first-stage washing kettle 7, the bottom of the second-stage washing kettle 10 is provided with the washing liquid discharge pipeline connected with the second-stage washing separator 11, the water phase discharge pipeline of the second-stage washing separator 11 is connected with the first-stage washing water storage tank 8, the organic phase discharge pipeline of the second-stage washing separator 11 is connected with the washing material storage tank 12, the organic phase discharge pipeline of the second-stage washing separator 11, the water phase discharge pipeline and the bottom washing liquid discharge pipeline of the second-stage washing kettle 10 are provided with the automatic control valves.
The washing material storage tank 12 is connected with a washing material preheater 14 through a pipeline, a flowmeter, a pump and an automatic control valve are arranged on the pipeline, the washing material preheater 14 is connected with a water benzene distillation tower 15 through the automatic control valve and the flowmeter, a water benzene steam pipeline of the water benzene distillation tower 15 is connected with a water benzene condenser 16 through the automatic control valve, a condensate outlet pipeline of the benzene condenser 16 is connected with a water benzene continuous separator 17 through the automatic control valve, a benzene outlet pipeline of the water benzene continuous separator 17 is connected with a benzene recovery tank 18 through the automatic control valve, and an outlet pipeline of the benzene recovery tank 18 is connected with a benzene transfer tank 19 through the automatic control valve.
The crude material outlet pipeline at the bottom of the water benzene distillation tower 15 is connected with a light component removal tower 20 through an automatic control valve, the benzene and low boiling point gas outlet pipeline of the light component removal tower 20 is connected with a light component removal condenser 21 through an automatic control valve, the liquid outlet pipe of the light component removal condenser 21 is connected with a washing material storage tank through an automatic control valve, the crude material outlet pipeline of the light component removal tower 20 is connected with a rectifying tower 22 through an automatic control valve, the benzophenone steam outlet pipeline of the rectifying tower 22 is connected with a rectifying condenser 23 through an automatic control valve, the rectifying condenser 23 is connected with a rectifying reflux groove 24 through an automatic control valve, the rectifying reflux groove 24 is connected with the reflux port of the rectifying tower 22 through a benzophenone reflux pipeline, the benzophenone reflux pipeline is provided with an automatic control valve and a flowmeter, and the rectifying reflux groove 24 is further connected with a benzophenone finished product groove 25 through an automatic control valve.
A raffinate discharge pipeline of the rectifying tower 22 is connected to a raffinate distiller 26, a steam outlet pipeline of the raffinate distiller 26 is connected to a benzophenone condenser 27 through an automatic control valve, a light fraction outlet of the benzophenone condenser 27 is connected to a light fraction receiving tank 29 through an automatic control valve, and a benzophenone outlet of the benzophenone condenser 27 is connected to a benzophenone receiving tank 28 through an automatic control valve. The residue of the residual liquid distillation kettle 26 enters a residual liquid hot washing kettle 30, and a waste water outlet pipeline of the residual liquid hot washing kettle 30 is connected with a residual liquid waste water tank 31 through an automatic control valve. And (4) removing water from the wastewater treatment station, and transferring the residues to incineration treatment.
Although embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that changes, modifications, substitutions and alterations can be made in these embodiments without departing from the principles and spirit of the utility model, the scope of which is defined in the appended claims and their equivalents.
Claims (6)
1. The utility model provides a benzophenone serialization production system, is including hydrolysising the stock chest and the neutralization kettle, be provided with agitating unit, its characterized in that in the neutralization kettle: the hydrolysis storage tank is connected with the neutralization kettle through a flowmeter and an automatic control valve, an alkaline water adding pipeline is arranged on the neutralization kettle and is connected with an alkaline water elevated tank, a flowmeter and an automatic control valve are arranged on the alkaline water adding pipeline, a neutralization liquid discharge pipeline is arranged at the bottom of the neutralization kettle and is connected with a neutralization continuous separator, an automatic control valve is arranged on the neutralization liquid discharge pipeline, a water phase discharge pipeline and an organic phase discharge pipeline are arranged on the neutralization continuous separator and are respectively connected with the hydrolysis water storage tank and the primary washing kettle, automatic control valves are respectively arranged on the water phase discharge pipeline and the organic phase discharge pipeline, a water inlet pipe of the primary washing kettle is connected with the primary washing water storage tank through the automatic control valve and the flowmeter, a discharge pipeline is arranged at the bottom of the primary washing kettle and is connected with the primary washing separator, a water phase discharge pipeline and an organic phase discharge pipeline are respectively arranged on the primary washing separator, the water phase discharge pipeline links to each other with the neutralizing water storage tank and the water storage tank of hydrolysising simultaneously to all be provided with automatic control valve, the neutralizing water storage tank links to each other with the neutralizing kettle, organic phase discharge pipeline links to each other with the second grade washing cauldron, all be provided with automatic control valve on the discharge pipeline of the water phase discharge pipeline of one-level washing separator, organic phase discharge pipeline and one-level washing cauldron, the bottom of second grade washing cauldron is provided with washing liquid discharge pipeline and links to each other with the second grade washing separator, the water phase discharge pipeline of second grade washing separator links to each other with the one-level washing water storage tank, the organic phase discharge pipeline of second grade washing separator links to each other with the washing material storage tank, all be provided with automatic control valve on the bottom washing liquid discharge pipeline of the organic phase discharge pipeline of second grade washing separator, water phase discharge pipeline and second grade washing cauldron.
2. The continuous benzophenone production system of claim 1, wherein: the alkaline water elevated tank is connected with the alkaline water preparation tank through a pipeline, and an automatic control valve and a flowmeter are arranged on the pipeline.
3. A continuous benzophenone production system as claimed in claim 1 or 2 wherein: the washing material storage tank passes through the pipeline and links to each other with washing material pre-heater, is provided with flowmeter and automatic control valve on this pipeline, washing material pre-heater passes through automatic control valve and flowmeter and links to each other with the water benzene distillation column, the water benzene steam pipeline of water benzene distillation column passes through automatic control valve and links to each other with the water benzene condenser, the condensate outlet pipeline of benzene condenser passes through automatic control valve and links to each other with water benzene continuous separation ware, water benzene continuous separation ware's benzene outlet pipeline passes through automatic control valve and links to each other with the benzene accumulator, the outlet pipeline of benzene accumulator passes through automatic control valve and links to each other with the benzene transfer tank.
4. The continuous benzophenone production system according to claim 3, wherein: the crude material outlet pipeline at the bottom of the water benzene distillation tower is connected with the light component removal tower through an automatic control valve, the benzene and low boiling point gas outlet pipeline of the light component removing tower is connected with a light component removing condenser through an automatic control valve, the liquid outlet pipe of the lightness-removing condenser is connected with the water washing material storage tank through an automatic control valve, the coarse material outlet pipeline of the lightness-removing tower is connected with the rectifying tower through the automatic control valve, the benzophenone steam outlet pipeline of the rectifying tower is connected with a rectifying condenser through an automatic control valve, the rectification condenser is connected with a rectification reflux tank through an automatic control valve, the rectification reflux tank is connected with a reflux port of a rectification tower through a benzophenone reflux pipeline, the benzophenone return line is provided with an automatic control valve and a flowmeter, and the rectification reflux tank is also connected with a benzophenone finished product tank through the automatic control valve.
5. The continuous benzophenone production system of claim 4, wherein: the raffinate discharge pipeline of rectifying column links to each other with the raffinate stills, the steam outlet pipeline of raffinate stills passes through automatic control valve and links to each other with the benzophenone condenser, the export of the light fraction of benzophenone condenser passes through automatic control valve and links to each other with the light fraction receiving tank, the benzophenone export of benzophenone condenser passes through automatic control valve and links to each other with the benzophenone receiving tank.
6. The continuous benzophenone production system of claim 5, wherein: and the residue of the residual liquid distillation kettle enters a residual liquid hot washing kettle, and a wastewater outlet pipeline of the residual liquid hot washing kettle is connected with a residual liquid wastewater tank through an automatic control valve.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202122719094.6U CN216538433U (en) | 2021-11-08 | 2021-11-08 | Benzophenone serialization production system |
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| CN202122719094.6U CN216538433U (en) | 2021-11-08 | 2021-11-08 | Benzophenone serialization production system |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115448828A (en) * | 2022-09-23 | 2022-12-09 | 重庆长风化学工业有限公司 | Production process of benzophenone and safe working method in production process |
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2021
- 2021-11-08 CN CN202122719094.6U patent/CN216538433U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115448828A (en) * | 2022-09-23 | 2022-12-09 | 重庆长风化学工业有限公司 | Production process of benzophenone and safe working method in production process |
| CN115448828B (en) * | 2022-09-23 | 2023-11-10 | 重庆长风化学工业有限公司 | Production process of diphenyl ketone and safe working method in process |
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