CN113979841A - Method for continuously producing chlorphenesin - Google Patents
Method for continuously producing chlorphenesin Download PDFInfo
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- CN113979841A CN113979841A CN202111358971.XA CN202111358971A CN113979841A CN 113979841 A CN113979841 A CN 113979841A CN 202111358971 A CN202111358971 A CN 202111358971A CN 113979841 A CN113979841 A CN 113979841A
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C37/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom of a six-membered aromatic ring
- C07C37/64—Preparation of O-metal compounds with O-metal group bound to a carbon atom belonging to a six-membered aromatic ring
- C07C37/66—Preparation of O-metal compounds with O-metal group bound to a carbon atom belonging to a six-membered aromatic ring by conversion of hydroxy groups to O-metal groups
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C41/00—Preparation of ethers; Preparation of compounds having groups, groups or groups
- C07C41/01—Preparation of ethers
- C07C41/16—Preparation of ethers by reaction of esters of mineral or organic acids with hydroxy or O-metal groups
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00002—Chemical plants
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- B01J2219/00033—Continuous processes
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Abstract
The invention discloses a method for continuously producing chlorphenesin, which comprises the following steps: step 1) in a first reactor, the molar ratio of 1: 1.0-1.5 of adding p-chlorophenol and an inorganic alkali solution to react; step 2) feeding the solution obtained in step 1) into a second reactor connected in series with the first reactor, in which the reaction is carried out according to the reaction conditions of p-chlorophenol: 3-chloro-1, 2-propanediol: the inorganic alkali solution is 1: 1.0-1.2: adding 3-chloro-1,2-propanediol in a molar ratio of 1.0-1.5, and reacting; and 3) separating the feed liquid obtained in the step 2), and filtering, crystallizing, centrifuging and drying the separated organic phase to obtain the chlorphenesin. The invention realizes the high-efficiency, safe and reliable industrial continuous production of the chlorphenesin product by using the two-stage kettle type reactor, and simultaneously, the new production route is utilized to improve the synthesis yield of the chlorphenesin product and the product quality.
Description
Technical Field
The invention relates to the field of chemical processes, and particularly relates to a method for continuously producing chlorphenesin.
Background
Chlorphenesin, chlorophenol ether, chlorphenesin, and its molecular formula C9H11ClO3It is a fine chemical product, and can be widely used in medicine, daily chemical products and fine chemical products. The global cosmetic market is growing at a rate approaching 10% per year, and cosmetic preservatives are used in increasingly larger amounts as major additives in cosmetics. The chlorphenesin can be widely applied due to the advantages of the chlorphenesin product. Chlorphenesin is widely applied to the manufacture of medicinal toothpaste, nail polish, perfumed soap, shampoo products and skin care products at present. Chlorphenesin as a cosmetic preservative has the following advantages:
(1) the use concentration in the cosmetics is low;
(2) does not contain any free or combined formaldehyde, and has good tolerance to local skin or mucosa;
(3) the oxidation of fat is not increased, and protein is not denatured;
(4) has low toxicity and is also an effective component for resisting psoriasis.
As for the preparation technology of chlorphenesin, the prior art is mostly chemical preparation. For example, British patent GB628497 uses p-chlorophenol and glycidol as raw materials, and the raw materials are reacted in the presence of pyridine, and the product is obtained by refining the reaction product with chloroform or diethyl ether-petroleum ether after treatment. In the method, ether-petroleum ether is used as a post-treatment solvent, and the method is volatile, flammable and explosive and is not suitable for large-scale production. Chinese patent CN101445436A discloses a method for preparing chlorphenesin by using epoxy chloropropane and p-chlorophenol as raw materials and sulfuric acid as a catalyst, in the method, dilute sulfuric acid is used as an oxidant to prepare 3-chloro-1,2-propanediol first, and then chlorphenesin is synthesized. The method has various reaction steps, reduces the reaction yield, introduces corrosive solvents such as strong acid and the like, is relatively difficult to post-treat and is not suitable for large-scale production. Other methods in the prior art also have the problems of multiple material transferring steps, low reaction efficiency, high cost, only realization of intermittent production and the like. Therefore, a new method capable of realizing continuous production of chlorphenesin is continuously found to solve the problems in the conventional chlorphenesin production.
Disclosure of Invention
One aspect of the invention provides a method for continuously producing chlorphenesin, aiming at the defects of multiple steps, low reaction efficiency, high cost and only realization of intermittent production in the preparation method of chlorphenesin in the prior art.
The technical scheme provided by the invention is as follows:
a method for continuously producing chlorphenesin, which comprises the following steps:
step 1) in a first reactor, the molar ratio of 1: 1.0-1.5 of adding p-chlorophenol and an inorganic alkali solution to react;
step 2) feeding the solution obtained in step 1) into a second reactor connected in series with the first reactor, in which the reaction is carried out according to the reaction conditions of p-chlorophenol: 3-chloro-1, 2-propanediol: the inorganic alkali solution is 1: 1.0-1.2: adding 3-chloro-1,2-propanediol in a molar ratio of 1.0-1.5, and reacting;
and 3) separating the feed liquid obtained in the step 2), and filtering, crystallizing, centrifuging and drying the separated organic phase to obtain the chlorphenesin.
In the invention, the reaction equation for preparing the chlorphenesin is as follows:
preferably, in one embodiment of the present invention, the reactor is a tank reactor.
In the present invention, the first reactor or the second reactor may be optionally composed of any number of tank reactors. The number and volume of the series-connected kettles of the kettle-type series-connected reactor depend on the production scale and the residence time. The kettle type reactor is composed of one or more kettle type reactors, and when the kettle type reactor is composed of more than two kettle type reactors, the kettle type reactors are connected in series.
In the present invention, the reaction kettles of the two or more kettle-type reactors may be connected in series by any suitable connection means, such as a pipeline pump, an overflow pipe, etc. Preferably, in one embodiment of the present invention, the reaction vessels are connected to each other by an overflow pipe. Functional devices such as a pressure testing device, a temperature testing device, a flow rate testing device and the like can be added on or between the kettles according to needs, and are considered to be included in the protection scope of the invention.
In the present invention, the tank reactor may be any suitable commercially available chemical reaction tank, including, but not limited to, a carbon steel reaction tank, a stainless steel reaction tank, a steel-lined PE reaction tank, a steel-lined PTEF reaction tank, a steel-lined titanium reaction tank, and the like. Preferably, in one embodiment of the invention, the tank reactor uses urea grade stainless steel as the tank liner. The urea grade stainless steel kettle body liner may be disposed within the reaction kettle by any suitable method, or purchased as a finished product reaction kettle.
Preferably, in an embodiment of the present invention, the inorganic alkali solution is a sodium hydroxide solution and/or a potassium hydroxide solution.
In an embodiment of the present invention, the inorganic alkaline solution preferably has a mass concentration of 5% to 20%.
Preferably, in an embodiment of the present invention, the reaction temperature in the step 1) is 50 to 80 ℃, and the average residence time of the feed liquid is 5 to 10 minutes.
Preferably, in an embodiment of the present invention, the reaction temperature in the step 2) is 90 to 110 ℃ and the average residence time of the feed liquid is 30 to 100 minutes.
In the present invention, the reaction product feed liquid obtained in the above step 2) may be subjected to separation of organic phase and inorganic phase by any suitable means, for example, by extraction or standing for separation. In one embodiment of the invention, the organic phase is separated by still standing, cooling and demixing in a separation tank.
The above step of separating the organic phase may further comprise a step of washing the organic phase to remove impurities therein. Preferably, in one embodiment of the present invention, the organic phase is washed with distilled water.
In the present invention, the crystallization method in the above step 3) may be any suitable crystallization method. Preferably, in one embodiment of the present invention, the crystallization is performed using an ethanol-water system.
In the invention, the production process flow is shown in figure 1, and after the parachlorophenol and the inorganic alkali solution in the step 1) are mixed in advance, the mixed solution is continuously fed into the first reactor at a constant speed of 40-80 mL/min for reaction; and when the solution in the first reactor is full and starts to enter the second reactor, continuously and constantly feeding the 3-chloro-1,2-propanediol into the second reactor at the speed of 30-50 mL/min for reaction.
The invention has the beneficial effects that:
the invention realizes the high-efficiency, safe and reliable industrial continuous production of the chlorphenesin product by using the two-stage kettle type reactor, and simultaneously, the new production route is utilized to improve the synthesis yield of the chlorphenesin product and the product quality.
Drawings
FIG. 1 is a flow chart of a production process in an embodiment of the present invention.
Detailed Description
The invention discloses a method for continuously producing chlorphenesin, which can be realized by appropriately improving process parameters by a person skilled in the art by referring to the content in the text. It is expressly intended that all such alterations and modifications which are obvious to those skilled in the art are deemed to be incorporated herein by reference, and that the techniques of the invention may be practiced and applied by those skilled in the art without departing from the spirit, scope and range of equivalents of the invention.
In the present invention, unless otherwise specified, scientific and technical terms used herein have the meanings that are commonly understood by those skilled in the art. Throughout the specification and claims, unless explicitly stated otherwise, the word "comprise", or variations such as "comprises" or "comprising", will be understood to imply the inclusion of a stated element or component but not the exclusion of any other element or component. The terms "such as," "e.g.," and the like are intended to refer to exemplary embodiments and are not intended to limit the scope of the present disclosure.
Some terms appearing in the present invention are explained below.
The term "p-chlorophenol" also refers to p-chlorophenol (p-chlorophenol), 4-chlorophenol (4-chlorophenol), 4-chloro-1-hydroxybenzene, p-chlorohydroxybenzene (4-chloro-1-hydroxybenzene). The pure product is colorless crystal, and the industrial product is yellow or pink crystal or powder. Volatile and the vapor has an unpleasant pungent odor. Inflammable, slightly soluble in waterHas a solubility in water (20 deg.C) of 27.1g/L, and can be dissolved in benzene, ethanol, ether, glycerol, chloroform, fixed oil and volatile oil. A1% aqueous solution made litmus acidic, less acidic than phenol and stronger than benzene. The product is mainly used in the industries of pesticide, medicine, dye, plastics and the like, and also used as an ethanol color-changing agent, a refined mineral oil selective solvent, microscopic analysis and the like. The parachlorophenol is combustible in open fire and high heat, and is decomposed at high temperature to generate toxic and corrosive smoke. Has strong irritation to eyes, mucosa, respiratory tract and skin. It can be fatal after inhalation due to inflammation, edema, spasm of throat and bronchus, chemical pneumonia, and pulmonary edema. The toxicities are manifested by burning, cough, wheezing, laryngitis, headache and nausea. Molecular formula C6H5ClO。
The term "3-chloro-1, 2-propanediol", 3-chloro-1,2-propanediol, trivial name 3-chloro-1, 2-dihydroxypropane, formula C3H7CIO2And the molecular weight is 110.55. The substance is flammable and highly toxic, and is a suspected carcinogen. Poisoning may occur after inhalation, ingestion or percutaneous absorption. Has effects on lung, liver, kidney and brain. Inhalation of vapor can produce symptoms such as nausea, headache, dizziness, coma, and the like. Inhalation of vapor can cause pulmonary edema, and serious cases can cause death.
The term "chlorphenesin," also known as chlorphenesin, chlorophenol ether, chemical name 3- (4-chlorophenoxy) -1, 2-propanediol. Molecular formula C9H11ClO3White powder, bitter taste, molecular weight 202.63, slightly soluble in water, easily soluble in ethanol, melting point 78-81 deg.C.
In order to make those skilled in the art better understand the technical solution of the present invention, the following detailed description of the present invention is provided with reference to specific embodiments.
Example 1:
mixing p-chlorophenol and 10% sodium hydroxide solution in a batching kettle, conveying the mixture into a first reaction kettle 1 by a constant flow pump at a speed of 40mL/min, adding the p-chlorophenol and the sodium hydroxide according to a molar ratio of 1:1.1, reacting the p-chlorophenol and the sodium hydroxide in the reaction kettle 1 at a reaction temperature of 70 ℃, reacting for 10min, and then feeding the mixture into a second reaction kettle 2 connected with the reaction kettle 1 in series. When the feed liquid in the reaction kettle 1 is full and starts to flow into the reaction kettle 2, 3-chloro-1,2-propanediol is conveyed to the reaction kettle 2 by a constant flow pump at 30mL/min, and the etherification reaction is carried out on the 3-chloro-1,2-propanediol and sodium parachlorophenol generated in the reaction kettle 1 in the reaction kettle 2, wherein the reaction ratio of parachlorophenol: 3-chloro-1, 2-propanediol: the mass ratio of sodium hydroxide is 1:1.1:1.1, the reaction temperature is 90 ℃, and the residence time of the reaction liquid is 60 min. After the reaction of the feed liquid is finished, the feed liquid enters a separation tank through a discharge hole of the reaction kettle, the feed liquid is kept stand and cooled to be layered, then the upper aqueous phase is removed, and the lower organic phase is a crude product of chlorphenesin. Washing the crude product in a washing tank to remove inorganic salt impurities in the product, washing with distilled water, and filtering, crystallizing, centrifuging and drying the washed semi-finished chlorphenesin to obtain the product. The crystallization is carried out by using an ethanol-water system. The detection shows that the content is 99.9 percent and the yield is 98.9 percent. The whole process has high production efficiency, low operation cost, safety and reliability.
Example 2:
mixing parachlorophenol and 5% potassium hydroxide solution in a batching kettle, conveying the mixed solution into a first reaction kettle 1 by a constant flow pump at a speed of 50mL/min, adding the parachlorophenol and the potassium hydroxide according to a molar ratio of 1:1.0, reacting the parachlorophenol and the potassium hydroxide in the reaction kettle 1 at a reaction temperature of 80 ℃, reacting for 5min, and then feeding the reacted solution into a second reaction kettle 2 connected with the reaction kettle 1 in series. When the feed liquid in the reaction kettle 1 is full and starts to flow into the reaction kettle 2, the 3-chloro-1,2-propanediol is conveyed to the reaction kettle 2 by a constant flow pump at a rate of 50mL/min, and the 3-chloro-1,2-propanediol in the reaction kettle 2 and the potassium parachlorophenate generated in the reaction kettle 1 are subjected to etherification reaction, wherein the reaction rate of the p-chlorophenol: 3-chloro-1, 2-propanediol: the mass ratio of potassium hydroxide is 1:1.2:1.0, the reaction temperature is 90 ℃, and the residence time of the reaction liquid is 100 min. After the reaction of the feed liquid is finished, the feed liquid enters a separation tank through a discharge hole of the reaction kettle, the feed liquid is kept stand and cooled to be layered, then the upper aqueous phase is removed, and the lower organic phase is a crude product of chlorphenesin. Washing the crude product in a washing tank to remove inorganic salt impurities in the product, washing with distilled water, and filtering, crystallizing, centrifuging and drying the washed semi-finished chlorphenesin to obtain the product. The crystallization is carried out by using an ethanol-water system. The detection shows that the content is 99.9 percent and the yield is 96.8 percent. The whole process has high production efficiency, low operation cost, safety and reliability.
Example 3:
mixing parachlorophenol and 20% sodium hydroxide solution in a batching kettle, conveying the mixture into a first reaction kettle 1 by a constant flow pump at a speed of 80mL/min, adding the parachlorophenol and the sodium hydroxide according to a molar ratio of 1:1.5, reacting the parachlorophenol and the sodium hydroxide in the reaction kettle 1 at a reaction temperature of 50 ℃, reacting for 8min, and then feeding the mixture into a second reaction kettle 2 connected with the reaction kettle 1 in series. When the feed liquid in the reaction kettle 1 is full and starts to flow into the reaction kettle 2, 3-chloro-1,2-propanediol is conveyed to the reaction kettle 2 by a constant flow pump at 40mL/min, and the etherification reaction is carried out on the 3-chloro-1,2-propanediol and sodium parachlorophenol generated in the reaction kettle 1 in the reaction kettle 2, wherein the reaction ratio of parachlorophenol: 3-chloro-1, 2-propanediol: the mass ratio of sodium hydroxide is 1:1.0:1.5, the reaction temperature is 110 ℃, and the residence time of the reaction liquid is 30 min. After the reaction of the feed liquid is finished, the feed liquid enters a separation tank through a discharge hole of the reaction kettle, the feed liquid is kept stand and cooled to be layered, then the upper aqueous phase is removed, and the lower organic phase is a crude product of chlorphenesin. Washing the crude product in a washing tank to remove inorganic salt impurities in the product, washing with distilled water, and filtering, crystallizing, centrifuging and drying the washed semi-finished chlorphenesin to obtain the product. The crystallization is carried out by using an ethanol-water system. The detection shows that the content is 99.9 percent and the yield is 97.2 percent. The whole process has high production efficiency, low operation cost, safety and reliability.
Example 4:
mixing parachlorophenol and 15% sodium hydroxide solution in a batching kettle, conveying the mixture into a first reaction kettle 1 by a constant flow pump at a speed of 60mL/min, adding the parachlorophenol and the sodium hydroxide according to a molar ratio of 1:1.2, reacting the parachlorophenol and the sodium hydroxide in the reaction kettle 1 at a reaction temperature of 65 ℃, reacting for 8min, and then feeding the mixture into a second reaction kettle 2 connected with the reaction kettle 1 in series. When the feed liquid in the reaction kettle 1 is full and starts to flow into the reaction kettle 2, 3-chloro-1,2-propanediol is conveyed to the reaction kettle 2 by a constant flow pump at 30mL/min, and the etherification reaction is carried out on the 3-chloro-1,2-propanediol and sodium parachlorophenol generated in the reaction kettle 1 in the reaction kettle 2, wherein the reaction ratio of parachlorophenol: 3-chloro-1, 2-propanediol: the mass ratio of sodium hydroxide is 1:1.1:1.2, the reaction temperature is 100 ℃, and the residence time of the reaction liquid is 80 min. After the reaction of the feed liquid is finished, the feed liquid enters a separation tank through a discharge hole of the reaction kettle, the feed liquid is kept stand and cooled to be layered, then the upper aqueous phase is removed, and the lower organic phase is a crude product of chlorphenesin. Washing the crude product in a washing tank to remove inorganic salt impurities in the product, washing with distilled water, and filtering, crystallizing, centrifuging and drying the washed semi-finished chlorphenesin to obtain the product. The crystallization is carried out by using an ethanol-water system. The detection shows that the content is 99.9 percent and the yield is 98.3 percent. The whole process has high production efficiency, low operation cost, safety and reliability.
Comparative example 1:
adding p-chlorophenol, 3-chloro-1, 2-propylene glycol and 10% sodium hydroxide solution into a reaction kettle according to the molar ratio of 1:1.1:1.1, heating the reaction system to 106 ℃, reacting for 5 hours, allowing the material liquid to enter a separation tank through a discharge port of the reaction kettle after the material liquid is reacted, standing, cooling the material liquid to generate layering, removing an upper aqueous phase, and taking a lower organic phase as a crude chlorphenesin product. Washing the crude product in a washing tank to remove inorganic salt impurities in the product, washing with distilled water, and filtering, crystallizing, centrifuging and drying the washed semi-finished chlorphenesin to obtain the product. The crystallization is carried out by using an ethanol-water system. The detection shows that the content is 95.1 percent and the yield is 78.5 percent.
The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, various modifications and decorations can be made without departing from the principle of the present invention, and these modifications and decorations should also be regarded as the protection scope of the present invention.
Claims (10)
1. A method for continuously producing chlorphenesin is characterized by comprising the following steps:
step 1) in a first reactor, the molar ratio of 1: 1.0-1.5 of adding p-chlorophenol and an inorganic alkali solution to react;
step 2) feeding the solution obtained in step 1) into a second reactor connected in series with the first reactor, in which the reaction is carried out according to the reaction conditions of p-chlorophenol: 3-chloro-1, 2-propanediol: the inorganic alkali solution is 1: 1.0-1.2: adding 3-chloro-1,2-propanediol in a molar ratio of 1.0-1.5, and reacting;
and 3) separating the feed liquid obtained in the step 2), and filtering, crystallizing, centrifuging and drying the separated organic phase to obtain the chlorphenesin.
2. The method of claim 1, wherein the reactor is a tank reactor.
3. The process of claim 2, wherein the tank reactor is composed of one or more than two tank reactors, and when the tank reactor is composed of more than two tank reactors, the tank reactors are connected in series.
4. The method of claim 3, wherein the two or more tank reactors are connected by an overflow pipe.
5. The method according to claim 1, wherein the inorganic base solution is a sodium hydroxide solution and/or a potassium hydroxide solution.
6. The method according to claim 1, wherein the reaction temperature in the step 1) is 50-80 ℃, and the average residence time of the feed liquid is 5-10 minutes.
7. The method according to claim 1, wherein the reaction temperature in the step 2) is 90 to 110 ℃ and the average residence time of the feed liquid is 30 to 100 minutes.
8. The method of claim 1, further comprising the step of washing the separated organic phase prior to said filtering in step 3).
9. The method according to claim 1 or 5, wherein the inorganic alkali solution has a mass concentration of 5% to 20%.
10. The method according to claim 1, wherein the parachlorophenol and the inorganic alkaline solution in step 1) are premixed and then continuously fed into the first reactor at a constant rate of 40 to 80mL/min for reaction; and when the solution in the first reactor is full and starts to enter the second reactor, continuously and constantly feeding the 3-chloro-1,2-propanediol into the second reactor at the speed of 30-50 mL/min for reaction.
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Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103304380A (en) * | 2013-04-27 | 2013-09-18 | 中国中化股份有限公司 | Production process for continuously hydrolyzing and producing hydroquinone through multi-kettles in series |
| CN105016989A (en) * | 2015-08-18 | 2015-11-04 | 北京桑普生物化学技术有限公司 | Synthetic method of chlorobenzene glyceryl ether |
| CN108440253A (en) * | 2018-05-09 | 2018-08-24 | 广西大学 | A kind of method of green high-efficient selectivity synthesis Chlorphenesin |
| CN108640821A (en) * | 2018-04-10 | 2018-10-12 | 恒河材料科技股份有限公司 | A kind of the rubigan tertbutyl ether synthetic method and device of high-efficiency and continuous |
| CN109293483A (en) * | 2018-11-29 | 2019-02-01 | 湖北阿泰克生物科技股份有限公司 | A method of Chlorphenesin is prepared using microchannel continuous flow reactor |
| CN111056928A (en) * | 2019-12-30 | 2020-04-24 | 陕西省石油化工研究设计院 | Method for synthesizing chlorphenesin |
| CN113149818A (en) * | 2021-03-15 | 2021-07-23 | 菏泽新东方日化科技有限公司 | Preparation process of chlorphenesin |
| CN113185384A (en) * | 2021-04-23 | 2021-07-30 | 渭南畅通药化科技有限公司 | Synthesis method of high-purity odorless chlorphenesin |
-
2021
- 2021-11-17 CN CN202111358971.XA patent/CN113979841A/en active Pending
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103304380A (en) * | 2013-04-27 | 2013-09-18 | 中国中化股份有限公司 | Production process for continuously hydrolyzing and producing hydroquinone through multi-kettles in series |
| CN105016989A (en) * | 2015-08-18 | 2015-11-04 | 北京桑普生物化学技术有限公司 | Synthetic method of chlorobenzene glyceryl ether |
| CN108640821A (en) * | 2018-04-10 | 2018-10-12 | 恒河材料科技股份有限公司 | A kind of the rubigan tertbutyl ether synthetic method and device of high-efficiency and continuous |
| CN108440253A (en) * | 2018-05-09 | 2018-08-24 | 广西大学 | A kind of method of green high-efficient selectivity synthesis Chlorphenesin |
| CN109293483A (en) * | 2018-11-29 | 2019-02-01 | 湖北阿泰克生物科技股份有限公司 | A method of Chlorphenesin is prepared using microchannel continuous flow reactor |
| CN111056928A (en) * | 2019-12-30 | 2020-04-24 | 陕西省石油化工研究设计院 | Method for synthesizing chlorphenesin |
| CN113149818A (en) * | 2021-03-15 | 2021-07-23 | 菏泽新东方日化科技有限公司 | Preparation process of chlorphenesin |
| CN113185384A (en) * | 2021-04-23 | 2021-07-30 | 渭南畅通药化科技有限公司 | Synthesis method of high-purity odorless chlorphenesin |
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