CN109748442B - Waste liquid treatment process for synthesizing benzofuranone - Google Patents
Waste liquid treatment process for synthesizing benzofuranone Download PDFInfo
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Abstract
The invention discloses a waste liquid treatment process for synthesizing benzofuranone, which comprises the following steps: acidifying the washing liquid, and then evaporating in vacuum to recover crystals; collecting the residue of the concentration kettle, alkalifying and then acidifying, filtering at low temperature, acidifying the filtrate and evaporating the filtrate to obtain crystals, washing the filter cake with water, performing suction filtration, drying and recycling; the method collects the waste liquid generated in the synthesis process of the benzofuranone, recycles useful components in the waste liquid, minimizes toxic substances in the waste liquid, avoids environmental pollution, reduces the synthesis cost of the benzofuranone, and improves the economic benefit of the benzofuranone, and the content of o-chlorophenylacetic acid is less than or equal to 0.05%, the content of o-hydroxyphenylacetic acid is less than or equal to 0.05%, the content of copper ions is less than or equal to 0.001%, the content of chlorine ions is less than or equal to 0.001%, the content of toluene is less than or equal to 0.03%, and the content of the benzofuranone is less than or equal to 0.01.
Description
Technical Field
The invention relates to the technical field of organic synthesis post-treatment, in particular to a waste liquid treatment process for synthesizing benzofuranone.
Background
Azoxystrobin is a strobilurin fungicide or strobilurins analogue developed by prenatal corporation. The azoxystrobin can be used for spraying and seed treatment of cereals, rice, grapes, potatoes, vegetables, fruit trees and other crop stems and leaves, and can also be used for soil treatment. The azoxystrobin is safe to crops, has no phytotoxicity and is safe to underground water and environment when used under the recommended dosage. It has the features of high efficiency, broad spectrum, protection, treatment, elimination, penetration, systemic activity, etc. and has excellent activity on almost all fungal diseases. Azoxystrobin is a new agricultural fungicide with great development potential and market activity after triazole fungicides in the pesticide field. As few manufacturers for producing the product are provided in China, the azoxystrobin has a large market in China and has good development prospect.
Benzofuran-2 (3H) -ketone is an important intermediate for synthesizing strobilurin fungicide, a large amount of waste liquid is generated in the synthesis reaction of benzofuran-2 (3H) -ketone in the prior art, the waste liquid contains not only recyclable useful components but also organic toxic components, the safety of the surrounding environment is influenced by direct discharge, and how to recover the useful components in the waste liquid and reduce the toxic substances in the waste liquid is a problem of important attention of the post-treatment process of the waste liquid.
Disclosure of Invention
In order to solve the problems, the invention aims to collect the waste liquid generated in the synthesis process of the benzofuranone, and recycle the useful components in the waste liquid, thereby reducing the content of organic matters in the waste liquid, reducing the production cost and improving the economic benefit.
In order to realize the purpose of the invention, the adopted technical scheme is as follows: a waste liquid treatment process for synthesizing benzofuranone comprises the following specific steps:
1) acidification: transferring the water washing liquid obtained from the water washing kettle into an acidification kettle, dropwise adding dilute acid, starting stirring until the water washing liquid does not generate bubbles any more, then heating the acidification liquid to 60-80 ℃, stirring for 20-40 min, and transferring the acidification liquid into an evaporation kettle while the acidification liquid is hot;
2) evaporation: opening a vacuum system of the evaporation kettle, slowly heating to 80-90 ℃ in a vacuum state, starting stirring when the volume of liquid in the evaporation kettle is 2/3-4/5 of the volume of the evaporation kettle, and starting a condenser for condensation;
starting a circulating pump beside the evaporation kettle, spraying the liquid material at the bottom of the evaporation kettle into the kettle from the left side of the upper part of the evaporation kettle, stopping the circulating pump when the volume of the liquid in the evaporation kettle is 1/3-1/2 of the volume of the evaporation kettle, accelerating the stirring speed until the liquid in the evaporation kettle is evaporated to dryness, stopping stirring, evaporating wet crystals by using waste heat, and recovering the crystals after evaporation to dryness to be sold as a byproduct;
3) saponification: collecting residues of the evaporation kettle, adding excessive alkali liquor, heating the solution to 60-70 ℃, starting stirring, stopping stirring when the mixed solution is not layered and no precipitate is generated, and transferring the material to an acidification kettle while the mixed solution is hot;
4) acidification: spraying dilute acid into the acidification kettle from the top of the acidification kettle, starting stirring, starting a circulating pump at the side of the acidification kettle when the volume of the mixed solution is 1/4-1/3 of the volume of the acidification kettle, and conveying the mixed solution at the bottom of the acidification kettle to the top of the acidification kettle to be sprayed into the acidification kettle in a circulating manner;
when the volume of the mixed solution in the acidification kettle is 1/2-2/3 of the volume of the acidification kettle, stopping adding acid, continuously stirring and spraying, when more precipitates appear in the acidification kettle, stopping circularly spraying, continuously stirring until the precipitates in the acidification kettle are not increased any more, and transferring the mixed material into a low-temperature filter;
5) filtering: controlling the temperature of the low-temperature filter to be 5-20 ℃, vacuumizing the low-temperature filter, performing suction filtration on the mixed material, transferring a filter cake into a washing kettle, transferring filtrate into the acidification kettle in the step 1, and repeating the step 1 and the step 2;
6) washing with water: controlling the temperature in the washing kettle to be 10-20 ℃, spraying the mixture from the top of the washing kettle to be 10-20 ℃, starting stirring, repeatedly washing for 30-45 min, transferring the mixed material to a suction filter for rapid suction filtration, adding pure water again until the mixed material submerges solids after suction drying, then carrying out suction drying again for 2-3 times, and drying the solid material after suction drying;
7) drying: controlling the temperature in a drying oven to be 60-100 ℃, spreading the dried solid material into a thin layer, placing the thin layer in the drying oven to be dried for 2-5 hours, collecting the solid material, cooling to room temperature, and applying the solid material to the synthesis of the benzofuranone.
Further, in the step 1 of the waste liquid treatment process, the dilute acid is dilute sulfuric acid, and the volume fraction concentration of the dilute sulfuric acid is controlled to be 5-15%.
Further, the vacuum system in the step 2 of the waste liquid treatment process controls the vacuum to be more than-0.095 MPa.
Further, in the step 3 of the waste liquid treatment process, the alkali liquor is a sodium bicarbonate solution, a sodium hydroxide solution or a mixed solution of sodium bicarbonate and sodium hydroxide, and the mass fraction concentration of the alkali liquor is controlled to be 10-40%.
Further, in the step 4 of the waste liquid treatment process, the dilute acid is dilute sulfuric acid, and the volume fraction concentration of the dilute sulfuric acid is controlled to be 5-15%.
The invention has the beneficial effects that: the method collects the waste liquid generated in the synthesis process of the benzofuranone, recycles useful components in the waste liquid, minimizes toxic substances in the waste liquid, avoids environmental pollution, reduces the synthesis cost of the benzofuranone, and improves the economic benefit of the benzofuranone, and the content of o-chlorophenylacetic acid is less than or equal to 0.05%, the content of o-hydroxyphenylacetic acid is less than or equal to 0.05%, the content of copper ions is less than or equal to 0.001%, the content of chlorine ions is less than or equal to 0.001%, the content of toluene is less than or equal to 0.03%, and the content of the benzofuranone is less than or equal to 0.01.
Detailed Description
The technical solutions of the present invention will be described clearly and completely with reference to the following embodiments of the present invention, and it should be understood that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Example 1
A waste liquid treatment process for synthesizing benzofuranone comprises the following specific steps:
1) acidification: transferring the water washing solution obtained from the water washing kettle into an acidification kettle, dropwise adding dilute sulfuric acid with volume fraction concentration of 5%, starting stirring until the water washing solution does not generate bubbles any more, stopping dropwise adding, heating the acidification solution to 60 ℃, stirring for 20min, and transferring the acidification solution to an evaporation kettle while the acidification solution is hot;
2) evaporation: opening a vacuum system of the evaporation kettle, controlling the vacuum to be-0.1 MPa by the vacuum system, slowly heating to 80 ℃ in a vacuum state, starting stirring when the volume of liquid in the evaporation kettle is 2/3 of the volume of the evaporation kettle, and starting a condenser for condensation;
starting a circulating pump beside the evaporation kettle, spraying the liquid material at the bottom of the evaporation kettle into the kettle from the left side of the upper part of the evaporation kettle, stopping the circulating pump when the volume of the liquid in the evaporation kettle is 1/3 of the volume of the evaporation kettle, accelerating the stirring speed until the liquid in the evaporation kettle is evaporated to dryness, stopping stirring, evaporating wet crystals by using waste heat, recovering the crystals after evaporation to dryness, and selling the crystals as a byproduct;
3) saponification: collecting residues of the evaporation kettle, adding excessive sodium bicarbonate solution with the mass fraction concentration of 10%, heating the solution to 60 ℃, starting stirring, stopping stirring when the mixed solution is not layered any more and no precipitate is generated, and transferring the hot material to an acidification kettle;
4) acidification: spraying dilute sulfuric acid with volume fraction concentration of 5% into the acidification kettle from the top of the acidification kettle, starting stirring, starting a circulating pump at the side of the acidification kettle when the volume of the mixed solution is 1/4 of the volume of the acidification kettle, and conveying the mixed solution at the bottom of the acidification kettle to the top of the acidification kettle to be circularly sprayed into the acidification kettle;
when the volume of the mixed solution in the acidification kettle is 1/2 of the volume of the acidification kettle, stopping adding acid, continuously stirring and spraying, when more precipitates appear in the acidification kettle, stopping circularly spraying, continuously stirring until the precipitates in the acidification kettle are not increased any more, and then transferring the mixed material into a low-temperature filter;
5) filtering: controlling the temperature of the low-temperature filter to be 5 ℃, vacuumizing the low-temperature filter, performing suction filtration on the mixed material, transferring a filter cake into a washing kettle, transferring filtrate into the acidification kettle in the step 1, and repeating the step 1 and the step 2;
6) washing with water: controlling the temperature in the washing kettle to be 10 ℃, spraying the mixture from the top of the washing kettle to be 10 ℃, starting stirring, repeatedly washing for 30min, transferring the mixed material into a suction filter for rapid suction filtration, adding pure water again until the mixed material submerges solids after being drained, then draining, repeatedly performing for 2 times, and drying the solid material after being drained;
7) drying: controlling the temperature in a drying oven to be 60 ℃, spreading the solid material obtained by pumping to be a thin layer, placing the thin layer in the drying oven for drying for 5 hours, collecting the solid material, cooling to room temperature, and applying the solid material to the synthesis of the benzofuranone;
the detection shows that the discharged wastewater contains 0.05 percent of o-chlorophenylacetic acid, 0.05 percent of o-hydroxyphenylacetic acid, 0.001 percent of copper ions, 0.001 percent of chloride ions, 0.03 percent of toluene and 0.01 percent of benzofuranone.
Example 2
A waste liquid treatment process for synthesizing benzofuranone comprises the following specific steps:
1) acidification: transferring the water washing solution obtained from the water washing kettle into an acidification kettle, dropwise adding dilute sulfuric acid with the volume fraction concentration of 15%, starting stirring until the water washing solution does not generate bubbles any more, stopping dropwise adding, heating the acidification solution to 80 ℃, stirring for 40min, and transferring the acidification solution to an evaporation kettle while the acidification solution is hot;
2) evaporation: opening a vacuum system of the evaporation kettle, controlling the vacuum to be-0.1 MPa by the vacuum system, slowly heating to 90 ℃ in a vacuum state, starting stirring when the volume of liquid in the evaporation kettle is 4/5 of the volume of the evaporation kettle, and starting a condenser for condensation;
starting a circulating pump beside the evaporation kettle, spraying the liquid material at the bottom of the evaporation kettle into the kettle from the left side of the upper part of the evaporation kettle, stopping the circulating pump when the volume of the liquid in the evaporation kettle is 1/2 of the volume of the evaporation kettle, accelerating the stirring speed until the liquid in the evaporation kettle is evaporated to dryness, stopping stirring, evaporating wet crystals by using waste heat, recovering the crystals after evaporation to dryness, and selling the crystals as a byproduct;
3) saponification: collecting residues of the evaporation kettle, adding excessive sodium hydroxide solution with the mass fraction concentration of 40%, heating the solution to 70 ℃, starting stirring, stopping stirring when the mixed solution is not layered any more and no precipitate is generated, and transferring the hot material to an acidification kettle;
4) acidification: spraying dilute sulfuric acid with volume fraction concentration of 15% into the acidification kettle from the top of the acidification kettle, starting stirring, starting a circulating pump at the side of the acidification kettle when the volume of the mixed solution is 1/3 of the volume of the acidification kettle, and conveying the mixed solution at the bottom of the acidification kettle to the top of the acidification kettle to be circularly sprayed into the acidification kettle;
when the volume of the mixed solution in the acidification kettle is 2/3 of the volume of the acidification kettle, stopping adding acid, continuously stirring and spraying, when more precipitates appear in the acidification kettle, stopping circularly spraying, continuously stirring until the precipitates in the acidification kettle are not increased any more, and then transferring the mixed material into a low-temperature filter;
5) filtering: controlling the temperature of the low-temperature filter to be 20 ℃, vacuumizing the low-temperature filter, performing suction filtration on the mixed material, transferring a filter cake into a washing kettle, transferring filtrate into the acidification kettle in the step 1, and repeating the step 1 and the step 2;
6) washing with water: controlling the temperature in the washing kettle to be 20 ℃, spraying the mixture from the top of the washing kettle to be 20 ℃, starting stirring, repeatedly washing for 45min, transferring the mixed material into a suction filter for rapid suction filtration, adding pure water again until the mixed material submerges solids after suction drying, then carrying out suction drying again for 3 times, and drying the solid material after suction drying;
7) drying: controlling the temperature in a drying oven to be 10 ℃, spreading the solid material obtained by pumping to be a thin layer, placing the thin layer in the drying oven for drying for 2 hours, collecting the solid material, cooling to room temperature, and applying the solid material to the synthesis of benzofuranone;
the detection shows that the discharged wastewater contains 0.045% of o-chlorophenylacetic acid, 0.035% of o-hydroxyphenylacetic acid, 0.0008% of copper ions, 0.0008% of chloride ions, 0.01% of toluene and 0.005% of benzofuranone.
Example 3
A waste liquid treatment process for synthesizing benzofuranone comprises the following specific steps:
1) acidification: transferring the water washing solution obtained from the water washing kettle into an acidification kettle, dropwise adding dilute sulfuric acid with the volume fraction concentration of 10%, starting stirring until the water washing solution does not generate bubbles any more, stopping dropwise adding, heating the acidification solution to 70 ℃, stirring for 30min, and transferring the acidification solution to an evaporation kettle while the acidification solution is hot;
2) evaporation: opening a vacuum system of the evaporation kettle, controlling the vacuum to be-0.1 MPa by the vacuum system, slowly heating to 85 ℃ in a vacuum state, starting stirring when the volume of liquid in the evaporation kettle is 4/5 of the volume of the evaporation kettle, and starting a condenser for condensation;
starting a circulating pump beside the evaporation kettle, spraying the liquid material at the bottom of the evaporation kettle into the kettle from the left side of the upper part of the evaporation kettle, stopping the circulating pump when the volume of the liquid in the evaporation kettle is 1/2 of the volume of the evaporation kettle, accelerating the stirring speed until the liquid in the evaporation kettle is evaporated to dryness, stopping stirring, evaporating wet crystals by using waste heat, recovering the crystals after evaporation to dryness, and selling the crystals as a byproduct;
3) saponification: collecting residues of an evaporation kettle, adding excessive sodium bicarbonate solution and sodium hydroxide solution with the mass fraction concentration of 20% or mixed solution of sodium bicarbonate and sodium hydroxide, heating the solution to 65 ℃, starting stirring, stopping stirring when the mixed solution is not layered any more and no precipitate is generated, and transferring the material to an acidification kettle while the mixed solution is hot;
4) acidification: spraying dilute sulfuric acid with the volume fraction concentration of 10% into the acidification kettle from the top of the acidification kettle, starting stirring, starting a circulating pump at the side part of the acidification kettle when the volume of the mixed solution is 1/3 of the volume of the acidification kettle, and conveying the mixed solution at the bottom of the acidification kettle to the top of the acidification kettle to be circularly sprayed into the acidification kettle;
when the volume of the mixed solution in the acidification kettle is 2/3 of the volume of the acidification kettle, stopping adding acid, continuously stirring and spraying, when more precipitates appear in the acidification kettle, stopping circularly spraying, continuously stirring until the precipitates in the acidification kettle are not increased any more, and then transferring the mixed material into a low-temperature filter;
5) filtering: controlling the temperature of the low-temperature filter to be 15 ℃, vacuumizing the low-temperature filter, performing suction filtration on the mixed material, transferring a filter cake into a washing kettle, transferring filtrate into the acidification kettle in the step 1, and repeating the step 1 and the step 2;
6) washing with water: controlling the temperature in the washing kettle to be 15 ℃, spraying the mixture from the top of the washing kettle to be 15 ℃, starting stirring, repeatedly washing for 40min, transferring the mixed material into a suction filter for rapid suction filtration, adding pure water again until the mixed material submerges solids after being drained, then draining, repeatedly performing for 3 times, and drying the solid material after being drained;
7) drying: controlling the temperature in a drying oven to be 80 ℃, spreading the solid material obtained by pumping to be a thin layer, placing the thin layer in the drying oven for drying for 4 hours, collecting the solid material, cooling to room temperature, and applying the solid material to the synthesis of the benzofuranone;
the detection shows that the content of o-chlorophenylacetic acid, o-hydroxyphenylacetic acid, copper ions, chlorine ions and benzofuranone in the discharged wastewater is 0.025%, 0.035%, 0.0009%, 0.001%, 0.01% and 0.008%.
The method collects the waste liquid generated in the synthesis process of the benzofuranone, recycles useful components in the waste liquid, minimizes toxic substances in the waste liquid, avoids environmental pollution, reduces the synthesis cost of the benzofuranone, and improves the economic benefit of the benzofuranone, and the content of o-chlorophenylacetic acid is less than or equal to 0.05%, the content of o-hydroxyphenylacetic acid is less than or equal to 0.05%, the content of copper ions is less than or equal to 0.001%, the content of chlorine ions is less than or equal to 0.001%, the content of toluene is less than or equal to 0.03%, and the content of the benzofuranone is less than or equal to 0.01.
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 invention, the scope of which is defined in the appended claims and their equivalents.
Claims (5)
1. A waste liquid treatment process for synthesizing benzofuranone is characterized by comprising the following steps: the waste liquid treatment process comprises the following specific steps:
1) acidification: transferring the water washing liquid obtained from the water washing kettle into an acidification kettle, dropwise adding dilute acid, starting stirring until the water washing liquid does not generate bubbles any more, then heating the acidification liquid to 60-80 ℃, stirring for 20-40 min, and transferring the acidification liquid into an evaporation kettle while the acidification liquid is hot;
2) evaporation: opening a vacuum system of the evaporation kettle, slowly heating to 80-90 ℃ in a vacuum state, starting stirring when the volume of liquid in the evaporation kettle is 2/3-4/5 of the volume of the evaporation kettle, and starting a condenser for condensation;
starting a circulating pump beside the evaporation kettle, spraying the liquid material at the bottom of the evaporation kettle into the kettle from the left side of the upper part of the evaporation kettle, stopping the circulating pump when the volume of the liquid in the evaporation kettle is 1/3-1/2 of the volume of the evaporation kettle, accelerating the stirring speed until the liquid in the evaporation kettle is evaporated to dryness, stopping stirring, evaporating wet crystals by using waste heat, and recovering the crystals after evaporation to dryness to be sold as a byproduct;
3) saponification: collecting residues of the evaporation kettle, adding excessive alkali liquor, heating the solution to 60-70 ℃, starting stirring, stopping stirring when the mixed solution is not layered and no precipitate is generated, and transferring the material to an acidification kettle while the mixed solution is hot;
4) acidification: spraying dilute acid into the acidification kettle from the top of the acidification kettle, starting stirring, starting a circulating pump at the side of the acidification kettle when the volume of the mixed solution is 1/4-1/3 of the volume of the acidification kettle, and conveying the mixed solution at the bottom of the acidification kettle to the top of the acidification kettle to be sprayed into the acidification kettle in a circulating manner;
when the volume of the mixed solution in the acidification kettle is 1/2-2/3 of the volume of the acidification kettle, stopping adding acid, continuously stirring and spraying, when more precipitates appear in the acidification kettle, stopping circularly spraying, continuously stirring until the precipitates in the acidification kettle are not increased any more, and transferring the mixed material into a low-temperature filter;
5) filtering: controlling the temperature of the low-temperature filter to be 5-20 ℃, vacuumizing the low-temperature filter, performing suction filtration on the mixed material, transferring a filter cake into a washing kettle, transferring filtrate into the acidification kettle in the step 1, and repeating the step 1 and the step 2;
6) washing with water: controlling the temperature in the washing kettle to be 10-20 ℃, spraying the mixture from the top of the washing kettle to be 10-20 ℃, starting stirring, repeatedly washing for 30-45 min, transferring the mixed material to a suction filter for rapid suction filtration, adding pure water again until the mixed material submerges solids after suction drying, then carrying out suction drying again for 2-3 times, and drying the solid material after suction drying;
7) drying: controlling the temperature in a drying oven to be 60-100 ℃, spreading the dried solid material into a thin layer, placing the thin layer in the drying oven to be dried for 2-5 hours, collecting the solid material, cooling to room temperature, and applying the solid material to the synthesis of the benzofuranone.
2. The process for treating waste liquid from the synthesis of benzofuranone as claimed in claim 1, wherein the process comprises the following steps: in the step 1 of the waste liquid treatment process, the dilute acid is dilute sulfuric acid, and the volume fraction concentration of the dilute sulfuric acid is controlled to be 5-15%.
3. The process for treating waste liquid from the synthesis of benzofuranone as claimed in claim 1, wherein the process comprises the following steps: in the step 2 of the waste liquid treatment process, the vacuum system controls the vacuum to be more than-0.095 MPa.
4. The process for treating waste liquid from the synthesis of benzofuranone as claimed in claim 1, wherein the process comprises the following steps: and in the step 3 of the waste liquid treatment process, the alkali liquor is a sodium bicarbonate solution, a sodium hydroxide solution or a mixed solution of sodium bicarbonate and sodium hydroxide, and the mass fraction concentration of the alkali liquor is controlled to be 10-40%.
5. The process for treating waste liquid from the synthesis of benzofuranone as claimed in claim 1, wherein the process comprises the following steps: in the step 4 of the waste liquid treatment process, the dilute acid is dilute sulfuric acid, and the volume fraction concentration of the dilute sulfuric acid is controlled to be 5-15%.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN106336388A (en) * | 2016-07-27 | 2017-01-18 | 重庆紫光国际化工有限责任公司 | Synthetic method of benzofuran-2(3H)-one |
| CN107417652A (en) * | 2017-04-13 | 2017-12-01 | 安徽广信农化股份有限公司 | A kind of synthesis technique of azoxystrobin intermediate benzofuranone |
| CN108002622A (en) * | 2017-11-16 | 2018-05-08 | 王小军 | A kind of method administered with remanufacture benzofuraxan waste liquid |
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106336388A (en) * | 2016-07-27 | 2017-01-18 | 重庆紫光国际化工有限责任公司 | Synthetic method of benzofuran-2(3H)-one |
| CN107417652A (en) * | 2017-04-13 | 2017-12-01 | 安徽广信农化股份有限公司 | A kind of synthesis technique of azoxystrobin intermediate benzofuranone |
| CN108002622A (en) * | 2017-11-16 | 2018-05-08 | 王小军 | A kind of method administered with remanufacture benzofuraxan waste liquid |
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