CN220443807U - Intermittent production system for 3-methoxy-N, N-dimethyl propionamide - Google Patents
Intermittent production system for 3-methoxy-N, N-dimethyl propionamide Download PDFInfo
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- CN220443807U CN220443807U CN202321972281.8U CN202321972281U CN220443807U CN 220443807 U CN220443807 U CN 220443807U CN 202321972281 U CN202321972281 U CN 202321972281U CN 220443807 U CN220443807 U CN 220443807U
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- 238000004519 manufacturing process Methods 0.000 title claims abstract description 45
- LBVMWHCOFMFPEG-UHFFFAOYSA-N 3-methoxy-n,n-dimethylpropanamide Chemical compound COCCC(=O)N(C)C LBVMWHCOFMFPEG-UHFFFAOYSA-N 0.000 title claims abstract description 39
- 238000006243 chemical reaction Methods 0.000 claims abstract description 39
- ROSDSFDQCJNGOL-UHFFFAOYSA-N Dimethylamine Chemical compound CNC ROSDSFDQCJNGOL-UHFFFAOYSA-N 0.000 claims description 30
- 239000002994 raw material Substances 0.000 claims description 29
- YSIKHBWUBSFBRZ-UHFFFAOYSA-N 3-methoxypropanoic acid Chemical compound COCCC(O)=O YSIKHBWUBSFBRZ-UHFFFAOYSA-N 0.000 claims description 14
- 238000010923 batch production Methods 0.000 claims description 9
- 238000001704 evaporation Methods 0.000 claims description 5
- 230000008020 evaporation Effects 0.000 claims description 5
- 238000007670 refining Methods 0.000 claims description 4
- 239000003054 catalyst Substances 0.000 abstract description 11
- 239000000126 substance Substances 0.000 abstract description 3
- 239000013067 intermediate product Substances 0.000 abstract description 2
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 61
- PEDCQBHIVMGVHV-UHFFFAOYSA-N Glycerine Chemical compound OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 description 18
- BAPJBEWLBFYGME-UHFFFAOYSA-N Methyl acrylate Chemical compound COC(=O)C=C BAPJBEWLBFYGME-UHFFFAOYSA-N 0.000 description 10
- WQDUMFSSJAZKTM-UHFFFAOYSA-N Sodium methoxide Chemical compound [Na+].[O-]C WQDUMFSSJAZKTM-UHFFFAOYSA-N 0.000 description 10
- 238000006845 Michael addition reaction Methods 0.000 description 9
- 239000000047 product Substances 0.000 description 9
- 238000007112 amidation reaction Methods 0.000 description 7
- 235000011187 glycerol Nutrition 0.000 description 7
- 239000000203 mixture Substances 0.000 description 6
- 239000012530 fluid Substances 0.000 description 5
- 238000000034 method Methods 0.000 description 5
- 239000011259 mixed solution Substances 0.000 description 5
- 238000010438 heat treatment Methods 0.000 description 4
- BDJSOPWXYLFTNW-UHFFFAOYSA-N methyl 3-methoxypropanoate Chemical compound COCCC(=O)OC BDJSOPWXYLFTNW-UHFFFAOYSA-N 0.000 description 4
- 238000002360 preparation method Methods 0.000 description 4
- 230000008569 process Effects 0.000 description 4
- 239000002904 solvent Substances 0.000 description 4
- 238000001514 detection method Methods 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 238000004064 recycling Methods 0.000 description 3
- 238000010992 reflux Methods 0.000 description 3
- 238000005070 sampling Methods 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 description 2
- 239000012295 chemical reaction liquid Substances 0.000 description 2
- 239000007795 chemical reaction product Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 229920005862 polyol Polymers 0.000 description 2
- 150000003077 polyols Chemical class 0.000 description 2
- 239000011541 reaction mixture Substances 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 230000002194 synthesizing effect Effects 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 241001248531 Euchloe <genus> Species 0.000 description 1
- HBBGRARXTFLTSG-UHFFFAOYSA-N Lithium ion Chemical compound [Li+] HBBGRARXTFLTSG-UHFFFAOYSA-N 0.000 description 1
- 239000004952 Polyamide Substances 0.000 description 1
- 239000004642 Polyimide Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000011248 coating agent Substances 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 239000000975 dye Substances 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 229910002804 graphite Inorganic materials 0.000 description 1
- 239000010439 graphite Substances 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000000976 ink Substances 0.000 description 1
- 229910001416 lithium ion Inorganic materials 0.000 description 1
- 239000004745 nonwoven fabric Substances 0.000 description 1
- 239000003973 paint Substances 0.000 description 1
- 230000002572 peristaltic effect Effects 0.000 description 1
- 230000035699 permeability Effects 0.000 description 1
- 229920002647 polyamide Polymers 0.000 description 1
- 229920001721 polyimide Polymers 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 238000010791 quenching Methods 0.000 description 1
- 239000004065 semiconductor Substances 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 230000000638 stimulation Effects 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 150000005846 sugar alcohols Polymers 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-N sulfuric acid Substances OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 1
- 239000011345 viscous material Substances 0.000 description 1
- 238000005303 weighing Methods 0.000 description 1
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model belongs to the field of chemical industry, and discloses a 3-methoxy-N, N-dimethylpropionamide intermittent production system, which comprises a 3-methoxy propionate production unit and a 3-methoxy-N, N-dimethylpropionamide production unit; the 3-methoxy propionate production unit comprises a first reaction kettle and a first rectifying tower connected with the first reaction kettle, wherein the top of the first rectifying tower is connected with a first light component collecting subunit and a second light component collecting subunit; the outlet of the second light component collecting subunit is connected with the feed end of the 3-methoxy-N, N-dimethyl propionamide production unit; and an outlet of the tower kettle of the first rectifying tower is connected to an inlet of the first reaction kettle. The system performs double collection of temperature sectional tower top light components in a 3-methoxy propionate production unit aiming at a first rectifying tower, performs catalyst collection in a tower kettle, and recycles the catalyst to a first reaction kettle; the intermediate product is collected and the catalyst is recycled.
Description
Technical Field
The utility model belongs to the field of new energy, and particularly relates to a 3-methoxy-N, N-dimethyl propionamide intermittent production system.
Background
The 3-methoxy-N, N-dimethyl propionamide can be mixed with various solvents, can dissolve polymer polyamide to a high degree, has the characteristics of high solubility, high permeability, low viscosity and the like, has no stimulation to skin, and is safe and environment-friendly. Has wide application in the aspects of paint, ink, dye and semiconductor cleaning. In addition, the preparation of the lithium ion battery diaphragm base film, the preparation of the diaphragm coating, the preparation of the polyimide diaphragm, the non-woven fabric diaphragm and the like can be used as solvents, the performance of the solvent can be compared with that of acetone, and the problems of environmental protection, cost and health risks are solved.
CN101616889B discloses a process for the preparation of β -alkoxypropionamides, example 5 of which employs a non-neutralized production process, the michael addition reaction product (3-methoxypropionate) being directly used for the amidation reaction.
In the production process, if methanol is not removed from the Michael addition product, the subsequent reaction efficiency is reduced, the dimethylamine dosage is increased, and the like.
Therefore, the problem solved by the present project is: how to realize the separation of 3-methoxy propionate and the multiplexing of catalyst in the Michael addition reaction in the production process of 3-methoxy-N, N-dimethylpropionamide.
Disclosure of Invention
Aiming at the defects of the prior art, the utility model aims to provide a 3-methoxy-N, N-dimethyl propionamide intermittent production system, which is used for carrying out double collection of temperature sectional tower top light components in a 3-methoxy propionate production unit aiming at a first rectifying tower, carrying out catalyst collection in a tower kettle, and recycling the catalyst to a first reaction kettle; the intermediate product is collected and the catalyst is recycled.
It should be noted that: in the utility model, pipeline fittings such as valves, pumps and the like or conveying power equipment are not described, and as known in the art, valves are arranged on most pipelines in the chemical industry field, and the types of the valves can be freely selected according to the properties of fluid; a bypass valve should also be provided at some valve positions where importance or failure rate is high;
the container, the reactor and the tower are used for conveying and refluxing materials, and the like, the machine pump is basically used in the field, the fluid flow can be realized by adopting a mode based on the dead weight of the fluid when the material conveying speed is not strict in the aspects of material release and the like, and the machine pump is generally used for conveying the fluid in other places, and the type of the machine pump are various, such as a diaphragm pump, a centrifugal pump, a peristaltic pump, a graphite pump and the like.
A weighing module is arranged on most of the raw material tanks; a thermometer and a pressure gauge are arranged in the kettle and the tower; as is well known in the art, the tank should be provided with necessary accessories such as heating and/or cooling jackets, stirring power devices, level gauges, etc., and if the tank needs to be operated under pressure or reduced pressure, a pressurizing pipe or a vacuum pipe should be provided; generally, the top of the kettle is provided with a condenser which is a horizontal condenser, a vertical condenser or a combination of the two condensers; the rectifying tower is of a conventional design in the field, a heat source is arranged at the tower bottom, reflux is arranged at the tower top, and the rectifying tower is generally a packed tower; the temperature gauge, the pressure gauge and the like are arranged at different heights in the tower, and the rectifying tower is also provided with a vacuum tube if the rectifying tower has the requirement of reduced pressure distillation.
The foregoing are all conventional designs and will not be described in detail in the text description of the present utility model; in the drawings of the present utility model, the above-mentioned accessories and devices are partially labeled, and if not labeled, the present utility model is not represented by the fact that the above-mentioned accessories and devices are not provided.
In order to achieve the aim of the utility model, the utility model adopts the following technical scheme: a batch production system of 3-methoxy-N, N-dimethyl propionamide comprises a 3-methoxy propionate production unit and a 3-methoxy-N, N-dimethyl propionamide production unit;
the 3-methoxy propionate production unit comprises a first reaction kettle and a first rectifying tower connected with the first reaction kettle, wherein the top of the first rectifying tower is connected with a first light component collecting subunit and a second light component collecting subunit; the outlet of the second light component collecting subunit is connected with the feed end of the 3-methoxy-N, N-dimethyl propionamide production unit;
and an outlet of the tower kettle of the first rectifying tower is connected to an inlet of the first reaction kettle.
In contrast to the prior art, the utility model has the following beneficial effects:
according to the utility model, the rectifying tower is arranged, the first light component collecting subunit is used for collecting methanol, the second light component collecting subunit is used for collecting the mixture containing 3-methoxy propionate, and the mixture is sent to the 3-methoxy-N, N-dimethyl propionamide production unit for amidation reaction.
Drawings
FIG. 1 is a pipeline flow diagram of a 3-methoxypropionate production unit of the example;
FIG. 2 is a pipeline flow diagram of a 3-methoxy-N, N-dimethylpropionamide production unit of the example.
Detailed Description
The technical scheme of the utility model is further described by the following specific embodiments. It should be apparent to those skilled in the art that the examples are provided merely to aid in understanding the present utility model, and should not be taken as a specific limitation on the utility model.
Examples
Referring to fig. 1, a batch production system of 3-methoxy-N, N-dimethylpropionamide comprises a 3-methoxypropionate production unit 100, a 3-methoxy-N, N-dimethylpropionamide production unit 200;
the 3-methoxy propionate production unit 100 comprises a first reaction kettle 101 and a first rectifying tower 102 connected with the first reaction kettle 101, wherein the top of the first rectifying tower 102 is connected with a first light component collecting subunit and a second light component collecting subunit; the outlet of the second light component collecting subunit is connected with the feed end of the 3-methoxy-N, N-dimethyl propionamide production unit 200;
the outlet of the tower kettle of the first rectifying tower 102 is connected to the inlet of the first reaction kettle 101.
Regarding the Michael addition reaction of the 3-methoxypropionate production unit 100 of the present embodiment, the amidation reaction of the 3-methoxy-N, N-dimethylpropionamide production unit 200 is carried out by the following specific process flow:
the Michael addition reaction comprises the following steps:
step 1: synthesizing, namely, taking methyl acrylate and methanol as raw materials, and carrying out Michael addition reaction in a first reaction kettle 101 in the presence of an unsupported alkaline catalyst such as sodium methoxide to obtain a first mixed solution containing 3-methoxy methyl propionate;
step 2: the methanol is removed by the first rectifying column 102 to obtain a mixture containing methyl 3-methoxypropionate.
More detailed description:
in the first reaction vessel 101, according to methyl acrylate: anhydrous methanol: the molar ratio of sodium methoxide is 1:2.5:0.4% and 108g of sodium methoxide (2 mol), 40kg of methanol (1250 mol) and 43kg of methyl acrylate (500 mol) are added at room temperature.
The reaction was stirred at 50℃for 2 hours, and after the completion of the reaction, the reaction mixture became clear and transparent in appearance. And (3) sampling, adding concentrated sulfuric acid to quench the reaction, performing GC detection, measuring that the content of methyl acrylate is lower than 1% and the sum of the content of other impurities is lower than 0.5%, then performing reduced pressure distillation in a first rectifying tower 102 under the vacuum degree of-0.095 MPa, heating the reaction liquid to 50 ℃, collecting methanol, gradually increasing the temperature to 80 ℃ along with the reduction of fractions, continuously collecting distilled liquid until no fractions are generated, and sampling for GC detection. Continuously heating to 90deg.C, vacuum distilling under-0.098 MPa, and collecting 68-73deg.C fraction; the condensate at the top of the tower in the temperature section of 50 ℃, 80 ℃ and 90 ℃ is collected by the first light component collecting subunit, and at the moment, the valve of the second light component collecting subunit is in a closed state;
and gradually increasing the temperature to 120 ℃ along with the reduction of the fraction, continuously collecting the fraction, sampling and performing GC detection to finally obtain 57kg of intermediate methyl 3-methoxypropionate with the purity of 99.86 percent, closing the first light component collecting subunit, and opening a valve of the second light component collecting subunit.
Only a little white solid sticky matter remains in the residue, and the main components are sodium methoxide and intermediate, and the sodium methoxide and the intermediate can be input into the first reaction kettle 101 for the next Michael addition reaction.
The specific procedure of the amidation reaction is described later.
Preferably, the 3-methoxypropionate production unit 100 further includes a first raw material tank 103, a second raw material tank 104, and a third raw material tank 105; the outlet of the first raw material tank 103, the outlet of the second raw material tank 104 and the outlet of the third raw material tank 105 are respectively connected to the inlet of the first reaction kettle 101; the outlet of the first light fraction collecting sub-unit communicates with a first feedstock tank 103.
The first raw material tank 103 is used for collecting methanol collected by the first rectifying tower 102; the second raw material tank 104 is for supplying methyl acrylate; the third raw material tank 105 is for supplying anhydrous methanol;
the residue in the tower kettle of the first rectifying tower 102 is not recommended to be directly used, and should be refined, specifically, a first refining subunit is arranged between the outlet of the tower kettle of the first rectifying tower 102 and the inlet of the first reaction kettle 101;
because the kettle residue is a white solid viscous substance, the kettle residue is preferably diluted before being refined so as to improve the fluid mobility and avoid the catalyst from being in a solid form, the solvent can be methanol, anhydrous methanol can be input through a pipeline, and the methanol of the first light component collecting subunit can also be adopted;
more preferably, the outlet of the first light component collecting sub-unit is connected to the body of the first rectifying column 102 by a pipe, methanol is injected into the first rectifying tower 102 in the later stage of rectification to dilute the residue.
In this embodiment, the first refining sub-unit comprises a first filter 106 and a first buffer tank 107 connected in sequence; the inlet of the first filter 106 is communicated with the outlet of the tower kettle of the first rectifying tower 102; the outlet of the first buffer tank 107 is communicated with the inlet of the first reaction kettle 101, and the inlet of the first buffer tank 107 is also communicated with the outlet of the first raw material tank 103.
The residue is filtered by the first filter 106, blended in the first buffer tank 107, methanol is introduced from the first raw material tank 103, the catalyst is diluted, and the diluted catalyst can be introduced into the first reaction tank 101 for reuse.
As a further refinement of the present embodiment, the first light component collecting subunit is a second buffer tank 108, and the second light component collecting subunit is a third buffer tank 109; the second buffer tank 108 and the third buffer tank 109 are connected in parallel, and a first condenser 110 is connected between an inlet of the second buffer tank 108, an inlet of the third buffer tank 109 and the top of the first rectifying tower 102; the outlet of the first condenser 110 is provided with a first return line 111 connected to the top of the first rectification column 102.
In some embodiments, two condensers may be provided at the top of the column, one condenser being connected to the second buffer tank 108 and one condenser being connected to the third buffer tank 109.
In the production process, both the collection of methanol and the collection of 3-methoxypropionate, it is common knowledge in the art that reflux is required, and this is not limited thereto.
Referring now to FIG. 2, which is a detailed description of a 3-methoxy-N, N-dimethylpropionamide production unit 200, which is similar to the piping arrangement of 3-methoxypropionate production unit 100, a great difference is that flash tank 202 is added, because the components of the reaction products are complex in the amidation reaction, and not only the raw materials (containing 3-methoxypropionate and methanol) fed from the Michael addition reaction, but also dimethylamine, product, and glycerol are removed by flash evaporation, and then the product, 3-methoxypropionate, and glycerol are separated in second rectifying column 203; it should be noted that a flash tank 202 may be provided between the first reaction tank 101 and the first rectifying column 102 in the 3-methoxypropionate production unit 100.
Specifically, the 3-methoxy-N, N-dimethyl propionamide production unit 200 comprises a second reaction kettle 201, a flash evaporation kettle 202 and a second rectifying tower 203 which are sequentially communicated; the outlet of the second light component collecting subunit is connected to the inlet of the second reaction kettle 201; the top of the second rectifying tower 203 is connected with an intermediate collecting subunit 204 and a product collecting subunit 205, and the intermediate collecting subunit 204 and the product collecting subunit 205 are both storage tanks. Intermediate collection subunit 204 is used to collect unreacted 3-methoxypropionate, and product collection subunit 205 is used to collect 3-methoxy-N, N-dimethylpropionamide;
the specific process of amidation reaction is as follows:
step 3: and synthesizing, namely carrying out amidation reaction on a second reaction kettle 201 by taking a mixture obtained by Michael addition reaction, polyol and dimethylamine as raw materials to obtain a second mixed solution containing 3-methoxy-N, N-dimethylpropionamide.
Step 4: the second mixed solution is subjected to light removal treatment in a flash evaporation kettle 202, and dimethylamine and methanol in the mixture are removed to obtain a third mixed solution;
step 5: the third mixture is decompressed, sectionally heated and rectified in a second rectifying tower 203, 3-methoxy propionate and 3-methoxy-N, N-dimethyl propionamide are respectively obtained in different temperature sections, and the tower bottom is polyalcohol;
and (3) recycling the 3-methoxy propionate and the polyol obtained in the step (5) to the step (3).
In more detail:
in the second reactor 201, methyl 3-methoxypropionate as an intermediate: dimethylamine: the molar ratio of glycerin is 1:2:1, 23.6kg of intermediate, 18.4kg of glycerol and 18kg of dimethylamine are added at 0 ℃. After the reaction was completed, the reaction mixture was transferred to flash tank 202, and was distilled under reduced pressure at-0.098 MPa and 45 ℃ to obtain a mixed solution of dimethylamine and methanol, which was then further separated in third rectifying column 211 (described later). And the rest reaction liquid is transferred into a second rectifying tower 203, the vacuum degree is minus 0.098MPa, the temperature is raised to 90 ℃, and the fraction in the temperature range of 65-80 ℃ is collected through an intermediate collecting subunit 204, and the fraction is mainly intermediate methyl 3-methoxypropionate. And continuously heating to 110 ℃, collecting fractions in a temperature range of 80-95 ℃ through a product collecting subunit 205, wherein the fractions are mainly 3-methoxy-N, N-dimethyl propionamide, and the residual kettle mainly comprises glycerol and can be recycled.
Specifically, the 3-methoxy-N, N-dimethylpropionamide production unit 200 further includes a fourth raw material tank 206, a dimethylamine supply module 207, and a fifth raw material tank 208; the outlet of the fourth raw material tank 206, the outlet of the dimethylamine supply module 207 and the outlet of the fifth raw material tank 208 are connected to the inlet of the second reaction kettle 201; the outlet of the bottom of the second rectifying column 203 is connected to the inlet of the fourth raw material tank 206.
The fourth raw material tank 206 is used for storing tower bottom liquid of the second rectifying tower 203, mainly glycerin;
the fifth raw material tank 208 is used for storing outsourced glycerin;
preferably, a second filter 209 is disposed between the outlet of the bottom of the second rectifying tower 203 and the inlet of the fourth raw material tank 206;
the intermediate collecting subunit 204 and the product collecting subunit 205 are connected in parallel; a second condenser 216 is arranged between the inlet of the intermediate collecting subunit 204, the inlet of the product collecting subunit 205 and the top of the second rectifying tower 203; the outlet of said second condenser 216 is provided with a second return line 217 connected to the top of the second rectifying column 203; the outlet of the intermediate collecting subunit 204 is connected to the inlet of the second reactor 201.
As can be seen from the above description of the detailed process details, the main substance collected by the intermediate collecting subunit 204 is 3-methoxypropionate as a component, and contains a small amount of methanol;
as a further preferred aspect of the present embodiment, a third condenser 210 and a third rectifying tower 211 that are sequentially connected are connected to the top of the flash tank 202, preferably, a sixth buffer tank 213 is disposed between the third condenser 210 and the third rectifying tower 211, a fourth condenser 212 is connected to the top of the third rectifying tower 211, and a fourth buffer tank 214 and a fifth buffer tank 215 that are connected in parallel are connected to the outlet of the fourth condenser 212; the fourth buffer tank 214 is connected to the dimethylamine supply module 207 and the fifth buffer tank 215 is connected to the first raw material tank 103.
The fourth buffer tank 214 is used for collecting dimethylamine, and the fifth buffer tank 215 is used for collecting methanol so as to realize the recycling of dimethylamine and methanol.
Claims (10)
1. A batch production system of 3-methoxy-N, N-dimethylpropionamide is characterized by comprising a 3-methoxy propionate production unit and a 3-methoxy-N, N-dimethylpropionamide production unit;
the 3-methoxy propionate production unit comprises a first reaction kettle and a first rectifying tower connected with the first reaction kettle, wherein the top of the first rectifying tower is connected with a first light component collecting subunit and a second light component collecting subunit; the outlet of the second light component collecting subunit is connected with the feed end of the 3-methoxy-N, N-dimethyl propionamide production unit;
and an outlet of the tower kettle of the first rectifying tower is connected to an inlet of the first reaction kettle.
2. The batch production system of 3-methoxy-N, N-dimethylpropionamide of claim 1, wherein the 3-methoxypropionate production unit further comprises a first feedstock tank, a second feedstock tank; the outlet of the first raw material tank and the outlet of the second raw material tank are respectively connected to the inlet of the first reaction kettle; the outlet of the first light component collecting subunit is communicated with a first raw material tank.
3. The batch 3-methoxy-N, N-dimethylpropionamide production system of claim 2, wherein the 3-methoxypropionate production unit further comprises a third feed tank, and an outlet of the third feed tank is communicated with an inlet of the first reaction tank.
4. The batch production system of 3-methoxy-N, N-dimethylpropionamide as set forth in claim 2, wherein a first refining subunit is disposed between the outlet of the first rectifying column bottom and the inlet of the first reaction kettle;
the first refining subunit comprises a first filter and a first buffer tank which are sequentially connected; the inlet of the first filter is communicated with the outlet of the tower kettle of the first rectifying tower; the outlet of the first buffer tank is communicated with the inlet of the first reaction kettle.
5. The batch 3-methoxy-N, N-dimethylpropionamide production system of claim 4, wherein the inlet of the first buffer tank is also in communication with the outlet of the first feed tank.
6. The batch production system of 3-methoxy-N, N-dimethylpropionamide of claim 1, wherein the first light component collection subunit is a second buffer tank and the second light component collection subunit is a third buffer tank; the second buffer tank and the third buffer tank are connected in parallel, and a first condenser is connected between an inlet of the second buffer tank, an inlet of the third buffer tank and the top of the first rectifying tower; the outlet of the first condenser is provided with a first return pipe connected to the top of the first rectifying tower.
7. The batch production system of 3-methoxy-N, N-dimethylpropionamide according to any one of claims 1 to 6, wherein the production unit of 3-methoxy-N, N-dimethylpropionamide comprises a second reaction kettle, a flash evaporation kettle and a second rectifying tower which are communicated in sequence; the outlet of the second light component collecting subunit is connected to the inlet of the second reaction kettle; the top of the second rectifying tower is connected with an intermediate collecting subunit and a product collecting subunit.
8. The batch production system of 3-methoxy-N, N-dimethylpropionamide of claim 7, wherein the 3-methoxy-N, N-dimethylpropionamide production unit further comprises a fourth feed tank, a dimethylamine supply module; the outlet of the fourth raw material tank and the outlet of the dimethylamine supply module are connected to the inlet of the second reaction kettle; and an outlet of the tower kettle of the second rectifying tower is connected to an inlet of the fourth raw material tank.
9. The batch production system of 3-methoxy-N, N-dimethylpropionamide as set forth in claim 8, wherein a filter is provided between the outlet of the bottom of the second rectifying column and the inlet of the fourth feed tank;
the intermediate collecting subunit and the product collecting subunit are connected in parallel; a second condenser is arranged among the inlet of the intermediate collecting subunit, the inlet of the product collecting subunit and the top of the second rectifying tower; the outlet of the second condenser is provided with a second return pipe connected to the top of the second rectifying tower;
the outlet of the intermediate collecting subunit is connected to the inlet of the second reaction kettle.
10. The intermittent production system of 3-methoxy-N, N-dimethyl propionamide according to claim 7, wherein a third condenser and a third rectifying tower which are sequentially communicated are connected to the flash evaporation kettle, a fourth condenser is connected to the top of the third rectifying tower, and a fourth buffer tank and a fifth buffer tank which are connected in parallel are connected to the outlet of the fourth condenser; the fourth buffer tank is connected to a dimethylamine supply module.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321972281.8U CN220443807U (en) | 2023-07-25 | 2023-07-25 | Intermittent production system for 3-methoxy-N, N-dimethyl propionamide |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321972281.8U CN220443807U (en) | 2023-07-25 | 2023-07-25 | Intermittent production system for 3-methoxy-N, N-dimethyl propionamide |
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| CN220443807U true CN220443807U (en) | 2024-02-06 |
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| CN202321972281.8U Active CN220443807U (en) | 2023-07-25 | 2023-07-25 | Intermittent production system for 3-methoxy-N, N-dimethyl propionamide |
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