CN218741906U - Production device for synthesizing tebuconazole intermediate - Google Patents
Production device for synthesizing tebuconazole intermediate Download PDFInfo
- Publication number
- CN218741906U CN218741906U CN202223182214.4U CN202223182214U CN218741906U CN 218741906 U CN218741906 U CN 218741906U CN 202223182214 U CN202223182214 U CN 202223182214U CN 218741906 U CN218741906 U CN 218741906U
- Authority
- CN
- China
- Prior art keywords
- cauldron
- recovery
- synthetic
- washing
- desolventizing
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model discloses a apparatus for producing that is used for ethylene oxide midbody of tebuconazole, including synthetic cauldron, washing cauldron, the desolventizing cauldron that connects gradually, be connected with the recovery cauldron between synthetic cauldron and the washing cauldron, the recovery cauldron passes through the reboiler and is connected with the synthetic cauldron, the recovery cauldron is connected with the top of washing cauldron through first condenser, the bottom of washing cauldron is passed through the recovery pump and is connected with the recovery cauldron, synthetic cauldron and feed tank group link, the desolventizing cauldron is connected with the finished product jar, the desolventizing cauldron still is connected with the recovery cauldron. The utility model recycles the waste water after washing, heats the waste water and provides heat for the synthesis kettle and the desolventizing kettle, reduces heat consumption, saves energy and reduces production cost; the utility model discloses utilize the condenser to dissolve the solvent recycle of cauldron, reduce the production consumption, reduce cost practices thrift the solvent, reduces the loss.
Description
Technical Field
The utility model relates to a chemical production technical field, concretely relates to apparatus for producing of synthetic tebuconazole intermediate.
Background
The 2- [2- (4-chlorphenyl) ethyl ] -2- (1, 1-dimethyl ethyl) oxirane is a key intermediate for synthesizing the pesticide tebuconazole, the tebuconazole is a triazole bactericidal pesticide with high efficiency, broad spectrum and systemic property, and has three functions of protection, treatment and eradication, wide bactericidal spectrum and long lasting period. The research finds that: tebuconazole, like all triazole fungicides, is able to inhibit the biosynthesis of fungal ergosterol. Tebuconazole is used as a seed treatment agent and foliar spray in the world, has a wide bactericidal spectrum, and not only has high activity but also has a long lasting period. The product can be used for preventing and treating sclerotinia rot of colza, and has the effects of resisting lodging, increasing yield, inhibiting demethylation of ergosterol on cell membrane, and killing bacteria.
Patent CN 110713472A discloses a synthesis method of 2- [2- (4-chlorophenyl) ethyl ] -2- (1, 1-dimethylethyl) oxirane, which comprises the steps of reacting a raw material A with dimethyl sulfate in the presence of a solvent, alkali and a catalyst to generate the product 2- [2- (4-chlorophenyl) ethyl ] -2- (1, 1-dimethylethyl) oxirane, washing with water, and desolventizing to obtain the product. The current production device needs a heating source in the synthesis and desolventizing steps, and the produced wastewater is not reused in the production device.
SUMMERY OF THE UTILITY MODEL
To the prior art, the utility model aims at providing a production device for synthesizing tebuconazole intermediate.
In order to achieve the above purpose, the utility model adopts the following technical scheme:
the utility model provides a production device of synthetic tebuconazole midbody, including synthetic cauldron, washing cauldron, the desolventizing cauldron that connects gradually, be connected with the recovery cauldron between synthetic cauldron and the washing cauldron, it passes through the reboiler and is connected with synthetic cauldron to retrieve the cauldron, it is connected with the top of washing cauldron through first condenser to retrieve the cauldron, the bottom of washing cauldron is passed through the recovery pump and is connected with the recovery cauldron, synthetic cauldron and feed tank group link, the desolventizing cauldron is connected with the finished product jar, the desolventizing cauldron still is connected with the recovery cauldron.
Preferably, the raw material tank group comprises a first raw material tank, a second raw material tank, a third raw material tank, a fourth raw material tank, a fifth raw material tank and a sixth raw material tank, the first raw material tank is connected with the top of the synthesis kettle through a flow meter, the second raw material tank is connected with the top of the synthesis kettle through a flow meter, the third raw material tank is connected with the top of the synthesis kettle through a flow meter, the fourth raw material tank is connected with the top of the synthesis kettle through a flow meter, the fifth raw material tank is connected with the top of the synthesis kettle through a flow meter, and the sixth raw material tank is connected with the top of the synthesis kettle through a flow meter and a dropping device in sequence.
Preferably, the desolventizing kettle is connected with a second condenser.
The utility model discloses a device is when producing 2- [2- (4-chlorphenyl) ethyl ] -2- (1, 1-dimethylethyl) oxirane, dimethyl sulfide in the first head tank, toluene in the second head tank, raw materials A in the third head tank, isopropanol in the fourth head tank are added simultaneously to the synthetic cauldron, then dimethyl sulfate is dripped into the synthetic cauldron through the dropwise add ware from the sixth head tank, potassium hydroxide gets into the synthetic cauldron from the fifth head tank after the dropwise add is accomplished, the reboiler heats the synthetic cauldron to 50 ℃, each raw materials takes place the reaction and produces 2- [2- (4-chlorphenyl) ethyl ] -2- (1, 1-dimethylethyl) oxirane, later 2- [2- (4-chlorphenyl) ethyl ] -2- (1, 1-dimethylethyl) oxirane gets into the top of water washing cauldron from the synthetic cauldron and washes, waste water after washing gets into the recovery cauldron through the recovery pump from the bottom of water washing cauldron and gets into the recovery cauldron from the recovery kettle, saturated steam provides the heat for the recovery cauldron with its water vapor first part after the distillation and gets back to the first water vapor recovery cauldron through the first (4-chlorphenyl) ethyl) -2- (1, the reboiler heats its water washing cauldron to the reboiler, it gets back to the first water recovery cauldron through the reboiler that the water gets back to 80 ℃ and gets into the heat recovery cauldron, it gets back to the water (1, the recovery cauldron and gets into the reboiler that water vapor recovery cauldron, the reboiler is heated water gets into the reboiler and gets into the first water is heated water of the recovery cauldron through the recovery cauldron, the reboiler; 2- [2- (4-chlorphenyl) ethyl ] -2- (1, 1-dimethyl ethyl) oxirane after washing enters a desolventizing kettle for desolventizing, and a finished product of the 2- [2- (4-chlorphenyl) ethyl ] -2- (1, 1-dimethyl ethyl) oxirane after desolventizing enters a finished product tank; and the solvent used for desolventizing enters a second condenser for condensation and then flows back to the desolventizing kettle.
The utility model has the advantages that:
the utility model recycles the waste water after washing, heats the waste water and provides heat for the synthesis kettle and the desolventizing kettle, reduces heat consumption, saves energy and reduces production cost; the utility model discloses utilize the condenser to dissolve the solvent recycle of cauldron, reduce the production consumption, reduce cost practices thrift the solvent, reduces the loss. The utility model discloses in only a heat source to with heat reuse, resources are saved.
The utility model is simple in operation, convenient to use, the production security is high, and the product yield is high, with waste water recycle, reduces heat consumption, will desolventize solvent recovery and reduce consumption.
Drawings
FIG. 1: the structure of the utility model is shown schematically;
shown in the figure: 1. the system comprises a synthesis kettle, 2 a recovery kettle, 3 a washing kettle, 4 a desolventizing kettle, 5 a finished product tank, 6 a second condenser, 7 a recovery pump, 8 a first condenser, 9 a reboiler, 10 a sixth raw material tank, 11 a fifth raw material tank, 12 a fourth raw material tank, 13 a third raw material tank, 14 a second raw material tank, 15 a first raw material tank, 16 a dropping device and 17 a flow meter.
Detailed Description
It should be noted that the following detailed description is exemplary and is intended to provide further explanation of the disclosure. Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this application belongs.
Just as the background art, based on this, the utility model provides a synthetic tebuconazole midbody's apparatus for producing, including synthetic cauldron 1, washing cauldron 3, the desolventizing cauldron 4 that connects gradually, be connected with between synthetic cauldron 1 and the washing cauldron 3 and retrieve cauldron 2, it is connected with synthetic cauldron 1 through reboiler 9 to retrieve cauldron 2, it is connected with washing cauldron 3's top through first condenser 8 to retrieve cauldron 2, washing cauldron 3's bottom is passed through recovery pump 7 and is connected with recovery cauldron 2, desolventizing cauldron 4 is connected with finished product jar 5, desolventizing cauldron 4 still is connected with recovery cauldron 2, desolventizing cauldron 4 is connected with second condenser 6.
Synthetic cauldron 1 and feed tank group link, the feed tank group includes first feed tank 15, second feed tank 14, third feed tank 13, fourth feed tank 12, fifth feed tank 11 and sixth feed tank 10, first feed tank 15 passes through flowmeter 17 and is connected with synthetic cauldron 1's top, second feed tank 14 passes through flowmeter 17 and is connected with synthetic cauldron 1's top, third feed tank 13 passes through flowmeter 17 and is connected with synthetic cauldron 1's top, fourth feed tank 12 passes through flowmeter 17 and is connected with synthetic cauldron 1's top, fifth feed tank 11 passes through flowmeter 17 and is connected with synthetic cauldron 1's top, sixth feed tank 10 loops through flowmeter 17, dripper 16 and is connected with synthetic cauldron 1's top.
In the production of 2- [2- (4-chlorophenyl) ethyl ] -2- (1, 1-dimethylethyl) oxirane, dimethyl sulfide in a first raw material tank 15, toluene in a second raw material tank 14, a raw material A in a third raw material tank 13 and isopropanol in a fourth raw material tank 12 are simultaneously added into a synthesis kettle 1, then the dimethyl sulfate is dripped into the synthesis kettle 1 from a sixth raw material tank 10 through a dripper 16, after the dropwise addition, potassium hydroxide enters a synthesis kettle 1 from a fifth raw material tank 11, a reboiler 9 heats the synthesis kettle 1 to 50 ℃, all raw materials react to generate 2- [2- (4-chlorophenyl) ethyl ] -2- (1, 1-dimethylethyl) oxirane, then the 2- [2- (4-chlorophenyl) ethyl ] -2- (1, 1-dimethylethyl) oxirane enters a washing kettle 3 from the synthesis kettle 1 to be washed, the washed wastewater flows out of the bottom of the washing kettle 3 and enters a recovery kettle 2 through a recovery pump 7, saturated steam provides heat for the recovery kettle 2 to heat the wastewater, and part of distilled water vapor returns to the washing kettle from the top of a distillation kettle 2 through a first condenser 8, washing 2- [2- (4-chlorphenyl) ethyl ] -2- (1, 1-dimethyl ethyl) ethylene oxide with water, feeding a part of water vapor into a reboiler 9 to heat the water vapor to 70-80 ℃, feeding heat to the synthesis kettle 1 by the reboiler 9 to heat the water vapor to 50 ℃, and feeding a part of the water vapor into the desolventizing kettle 4 to heat the water vapor; the 2- [2- (4-chlorphenyl) ethyl ] -2- (1, 1-dimethyl ethyl) oxirane after washing enters a desolventizing kettle 4 for desolventizing, a finished product of the 2- [2- (4-chlorphenyl) ethyl ] -2- (1, 1-dimethyl ethyl) oxirane after desolventizing enters a finished product tank 5, and a solvent used for desolventizing enters a second condenser 6 for condensing and then reflows to the desolventizing kettle 4.
In order to make the technical solutions of the present application more clearly understood by those skilled in the art, the technical solutions of the present application will be described in detail below with reference to specific embodiments.
The test materials used in the embodiment of the utility model are the conventional test materials in the field, and can be purchased through commercial channels.
Examples
The utility model provides a apparatus for producing of synthetic tebuconazole midbody, is connected with recovery cauldron 2 including synthetic cauldron 1, washing cauldron 3, desolventizing cauldron 4 that connect gradually between synthetic cauldron 1 and the washing cauldron 3, recovery cauldron 2 is connected with synthetic cauldron 1 through reboiler 9, recovery cauldron 2 is connected with washing cauldron 3's top through first condenser 8, washing cauldron 3's bottom is passed through recovery pump 7 and is connected with recovery cauldron 2, desolventizing cauldron 4 is connected with finished product jar 5, desolventizing cauldron 4 still is connected with recovery cauldron 2, desolventizing cauldron 4 is connected with second condenser 6.
Synthetic cauldron 1 and feed tank group link, the feed tank group includes first feed tank 15, second feed tank 14, third feed tank 13, fourth feed tank 12, fifth feed tank 11 and sixth feed tank 10, first feed tank 15 passes through flowmeter 17 and is connected with synthetic cauldron 1's top, second feed tank 14 passes through flowmeter 17 and is connected with synthetic cauldron 1's top, third feed tank 13 passes through flowmeter 17 and is connected with synthetic cauldron 1's top, fourth feed tank 12 passes through flowmeter 17 and is connected with synthetic cauldron 1's top, fifth feed tank 11 passes through flowmeter 17 and is connected with synthetic cauldron 1's top, sixth feed tank 10 loops through flowmeter 17, dropwise add ware 16 and is connected with synthetic cauldron 1's top.
In the production of 2- [2- (4-chlorophenyl) ethyl ] -2- (1, 1-dimethylethyl) oxirane, dimethyl sulfide in a first raw material tank 15, toluene in a second raw material tank 14, a raw material A in a third raw material tank 13 and isopropanol in a fourth raw material tank 12 are simultaneously added into a synthesis kettle 1, then the dimethyl sulfate is dripped into the synthesis kettle 1 from a sixth raw material tank 10 through a dripper 16, after the dropwise addition, potassium hydroxide enters a synthesis kettle 1 from a fifth raw material tank 11, a reboiler 9 heats the synthesis kettle 1 to 50 ℃, all raw materials react to generate 2- [2- (4-chlorophenyl) ethyl ] -2- (1, 1-dimethylethyl) oxirane, then the 2- [2- (4-chlorophenyl) ethyl ] -2- (1, 1-dimethylethyl) oxirane enters a washing kettle 3 from the synthesis kettle 1 to be washed, the washed wastewater flows out of the bottom of the washing kettle 3 and enters a recovery kettle 2 through a recovery pump 7, saturated steam provides heat for the recovery kettle 2 to heat the wastewater, and part of distilled water vapor returns to the washing kettle from the top of a distillation kettle 2 through a first condenser 8, washing 2- [2- (4-chlorphenyl) ethyl ] -2- (1, 1-dimethylethyl) ethylene oxide with water, feeding a part of water vapor into a reboiler 9 to heat the water vapor to 70-80 ℃, feeding heat from the reboiler 9 to the synthesis kettle 1 to heat the water vapor to 50 ℃, and feeding a part of water vapor into a desolventizing kettle 4 to supply heat to the water vapor; the 2- [2- (4-chlorphenyl) ethyl ] -2- (1, 1-dimethyl ethyl) oxirane after washing enters a desolventizing kettle 4 for desolventizing, a finished product of the 2- [2- (4-chlorphenyl) ethyl ] -2- (1, 1-dimethyl ethyl) oxirane after desolventizing enters a finished product tank 5, and a solvent used for desolventizing enters a second condenser 6 for condensing and then reflows to the desolventizing kettle 4.
The above description is only a preferred embodiment of the present application and is not intended to limit the present application, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, improvement and the like made within the spirit and principle of the present application shall be included in the protection scope of the present application.
Claims (3)
1. The utility model provides a apparatus for producing of synthetic tebuconazole midbody, its characterized in that, including synthetic cauldron, washing cauldron, the desolventizing cauldron that connects gradually, be connected with the recovery cauldron between synthetic cauldron and the washing cauldron, the recovery cauldron passes through the reboiler and is connected with synthetic cauldron, the recovery cauldron is connected with the top of washing cauldron through first condenser, the bottom of washing cauldron is passed through the recovery pump and is connected with the recovery cauldron, synthetic cauldron and feed tank group link, the desolventizing cauldron is connected with the finished product jar, the desolventizing cauldron still is connected with the recovery cauldron.
2. The apparatus for producing of synthetic tebuconazole intermediate of claim 1, characterized in that, feed tank group includes first feed tank, second feed tank, third feed tank, fourth feed tank, fifth feed tank and sixth feed tank, first feed tank passes through the flowmeter and is connected with the top of synthetic kettle, the second feed tank passes through the flowmeter and is connected with the top of synthetic kettle, third feed tank passes through the flowmeter and is connected with the top of synthetic kettle, the fourth feed tank passes through the flowmeter and is connected with the top of synthetic kettle, fifth feed tank passes through the flowmeter and is connected with the top of synthetic kettle, sixth feed tank loops through the flowmeter, the dripper is connected with the top of synthetic kettle.
3. The apparatus for producing a tebuconazole intermediate of claim 1, wherein the desolventizing still is connected with a second condenser.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202223182214.4U CN218741906U (en) | 2022-11-30 | 2022-11-30 | Production device for synthesizing tebuconazole intermediate |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202223182214.4U CN218741906U (en) | 2022-11-30 | 2022-11-30 | Production device for synthesizing tebuconazole intermediate |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN218741906U true CN218741906U (en) | 2023-03-28 |
Family
ID=85678507
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202223182214.4U Active CN218741906U (en) | 2022-11-30 | 2022-11-30 | Production device for synthesizing tebuconazole intermediate |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN218741906U (en) |
-
2022
- 2022-11-30 CN CN202223182214.4U patent/CN218741906U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN112076780B (en) | Catalytic preparation method of isopropanolamine | |
| CN106397329A (en) | Synthesis technology of allantoin | |
| CN218741906U (en) | Production device for synthesizing tebuconazole intermediate | |
| CN109651186B (en) | Device and process for producing powdery sodium cocoyl glycinate | |
| CN218834473U (en) | Synthesis system of tebuconazole competitive product | |
| CN106748696A (en) | A kind of preparation method of methylionone and its intermediate | |
| CN106220578A (en) | A kind of new benzoguanamine production method | |
| CN103848759A (en) | Method for applying esterification tail gas produced in synthesis of butyl isocyanate to salification | |
| CN107500460A (en) | A kind of ortho-nitraniline mother liquor processing method | |
| CN110002970B (en) | Production method and production system of sandalwood ether | |
| CN104262991B (en) | A kind of method of semi-continuous production white dyes | |
| CN207203493U (en) | Dimethylformamide evaporative applications device | |
| CN104292197A (en) | Synthesis method of spirodiclofen | |
| CN107880293A (en) | A kind of method that cellulose membrane is prepared using rice straw | |
| CN109748815A (en) | A kind of synthetic method of adipic dihydrazide | |
| CN105905928B (en) | A kind of handling process for preparing waste liquid during 3,6 dichlorosalicylic acids | |
| CN106608833B (en) | Ethanol amine co-production | |
| CN104610014A (en) | Method for preparing m-dichlorobenzene by catalyzing isomerization of p-dichlorobenzene by using nano ZSM-12 molecular sieve | |
| CN107522638A (en) | Prepare the microreactor and method of o-methyl formate benzene sulfonamide | |
| CN203976931U (en) | Energy-efficient equipment in succinic acid preparation | |
| Hofer | In Kaisten, syngenta operates the world's largest plant in which an enantioselective catalytic hydrogenation is performed. How did this come about? | |
| CN106608829B (en) | Ammonia recovery method in ethanol amine joint production process | |
| CN108546248B (en) | Preparation method of 1, 2-dihydro-3, 6-pyridazine dione | |
| CN106045864A (en) | Production process for preparing 4-chloro-2,5-dimethoxyaniline with hydrazine hydrate catalytic reduction method | |
| CN108129272A (en) | The system and method that a kind of microwave catalysis continuously prepares alcohol ether |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |