CN214973960U - Production device for preparing high-molecular polymer intermediate through esterification reaction - Google Patents
Production device for preparing high-molecular polymer intermediate through esterification reaction Download PDFInfo
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- CN214973960U CN214973960U CN202120661198.3U CN202120661198U CN214973960U CN 214973960 U CN214973960 U CN 214973960U CN 202120661198 U CN202120661198 U CN 202120661198U CN 214973960 U CN214973960 U CN 214973960U
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Abstract
The utility model discloses an esterification reaction system high molecular polymer midbody apparatus for producing, including esterification reaction unit, distillation reaction unit, catalyst recovery unit and product rectification unit, esterification reaction unit with the distillation reaction unit passes through the pipeline connection, the distillation reaction unit is provided with gas phase line and liquidus, the gas phase line with product rectification unit connection, the liquidus with catalyst recovery unit connection, product rectification unit is provided with discharge line and is connected with outside product tank district and produces the finished product, catalyst recovery unit is provided with discharge line and is connected with outside catalyst recovery tank and retrieves the catalyst, the utility model discloses a through a plurality of reactors continuous reaction, increased the reaction depth, realize the production serialization, prevent the polymerization of reactant through the hypoxic air, improved intermediate product and byproduct separation efficiency, and the DCS control system is adopted, so that the production level and the product quality of an enterprise are improved.
Description
Technical Field
The utility model relates to a chemical industry equipment field, concretely relates to esterification reaction system high molecular polymer midbody apparatus for producing.
Background
The high molecular polymer is a large class of water-soluble polymers with the widest application range at present, has high application value in the fields of petrochemical industry, papermaking, textile printing and dyeing, daily chemicals, particularly as a flocculating agent in the fields of water treatment, sludge dewatering and the like, and has the advantages of increasing the market demand year by year and good prospect. The production mode of the high molecular polymer mainly adopts the polymerization of cationic monomers such as quaternary ammonium salt, quaternary phosphonium salt, quaternary sulfonium salt and the like, wherein the mechanical force survivability of the DAC cationic polymer for forming floccules is far better than that of a DMC flocculant, and the high molecular flocculant is a high molecular flocculant product which is most widely applied and used at present. DA is a main intermediate for producing DAC cationic polymers at present, the quality of DA products directly influences the product quality and yield of the subsequent DAC cationic high-molecular polymers, and the quality of DA products depends on a production device for esterification.
Because the domestic complete equipment for realizing DA industrial production is less, compared with the patent device, the problems of insufficient reaction depth of a monomer reaction kettle, low separation precision and recovery rate of catalyst and device intermediate products, low automation control level, poor continuous production capacity, unstable product quality and the like exist, the high-quality DA production device is highly concerned by high polymer operating manufacturers due to the increase of the market demand of DAC cationic high polymer, therefore, the market needs to provide a production device for preparing a high polymer intermediate by esterification reaction to expand the productivity of DAC monomer, and meet the demand of high-quality DAC flocculant products at home and abroad.
SUMMERY OF THE UTILITY MODEL
The utility model aims at providing a production device for preparing a high molecular polymer intermediate by esterification reaction aiming at the defects existing in the prior art.
The technical scheme of the utility model is that:
the device comprises an esterification reaction unit, a distillation reaction unit, a catalyst recovery unit and a product rectification unit, wherein the esterification reaction unit is connected with the distillation reaction unit through a pipeline, the distillation reaction unit is provided with a gas phase line and a liquid phase line, the gas phase line is connected with the product rectification unit, the liquid phase line is connected with the catalyst recovery unit, the product rectification unit is provided with a discharge pipeline and is connected with an external product tank area to produce a finished product, and the catalyst recovery unit is provided with a discharge pipeline and is connected with an external catalyst recovery tank to recover a catalyst;
the esterification reaction unit comprises an esterification reaction kettle, a catalyst quantitative injection pump, a reaction heater and a material transferring pump, wherein the catalyst quantitative injection pump is connected with a feed inlet at the top of the esterification reaction kettle, the top of the esterification reaction kettle is also provided with a feed inlet for methyl acrylate, dimethylethanolamine and n-hexane, the bottom of the esterification reaction kettle is provided with a liquid phase pipeline and is connected with the material transferring pump, the material transferring pump is provided with a reflux outlet and a distillation outlet, the reaction heater is connected with the reflux outlet of the material transferring pump, the top of the reaction heater is connected with the top of the esterification reaction kettle, and the distillation reaction unit is connected with the distillation outlet of the material transferring pump.
Preferably, the top of the esterification reaction kettle is also connected with a methanol and alkane distillation recovery unit, and the methanol and alkane distillation recovery unit comprises a methanol distillation tower, a methanol distillation cooler, a methanol reflux tank, a methanol reflux pump, a n-hexane washing separation tank, a n-hexane intermediate tank and a n-hexane delivery pump;
the esterification reaction kettle, the methanol distillation tower, the methanol distillation cooler, the methanol reflux tank, the methanol reflux pump and the n-hexane washing separation tank are sequentially connected through a pipeline and enter the methanol distillation tower to form a methanol distillation recovery structure, the n-hexane washing separation tank is also provided with a deionized water feeding pipe, the lower part of the methanol distillation tower is also provided with a low-oxygen air feeding pipeline, and the middle part of the methanol distillation tower is provided with a pipeline and is connected with an external methanol water tank zone;
the esterification reaction kettle, the methanol distillation tower, the n-hexane intermediate tank and the n-hexane delivery pump are sequentially connected through pipelines and enter the esterification reaction kettle to form an alkane distillation recovery structure;
the methanol reflux pump is provided with a gas phase outlet and is connected with the methanol distillation tower, the n-hexane washing separation tank is provided with a liquidus and is connected with the n-hexane intermediate tank, and the n-hexane delivery pump is provided with a gas phase line and is connected with the n-hexane intermediate tank.
Preferably, the distillation reaction unit includes distillation reation kettle, distillation circulating pump and distillation cooler, the distillation reation kettle top be provided with the feed inlet and with the material transfer pump is connected, the distillation reation kettle lower part be provided with the liquid phase pipeline and with the distillation circulating pump is connected, the distillation circulating pump is provided with backward flow export and residue export, the distillation cooler with the backward flow exit linkage of distillation circulating pump, the distillation cooler with the distillation reation kettle is connected, catalyst recovery unit with the residue exit linkage of distillation circulating pump.
Preferably, the catalyst recovery unit includes distillation pump, catalyst stills, distillation residue pump, catalyst condenser and catalyst jar, distillation pump, catalyst stills, catalyst condenser and catalyst jar loop through the pipe connection, catalyst stills bottom with the distillation residue pump is connected, the distillation residue pump is provided with backward flow export and residue export, the catalyst stills with the backward flow exit linkage of distillation residue pump forms the backflow processing structure, the residue export of distillation residue pump is connected with outside distillation residue treatment zone and is discharged the residue.
Preferably, the product rectification unit comprises a product rectification tower, a product condenser, a reflux buffer tank, a rectification reflux pump, a product delivery pump, a product stabilization reaction kettle, a product stabilization reflux pump, a negative pressure buffer tank, a vacuum pump set, a liquid phase enrichment tank and a liquid phase enrichment tank pump, and a low-oxygen air pipeline is arranged at the lower part of the product distillation tower;
the distillation reaction kettle, the product rectifying tower, the product condenser, the reflux buffer tank and the rectifying reflux pump are sequentially connected through a pipeline and enter the distillation reaction kettle to form a product primary treatment circulating structure; the top of the product condenser is provided with a gas phase pipeline branch and is connected with the negative pressure buffer tank, the lower part of the reflux buffer tank is provided with a liquid phase pipeline branch and is connected with the product delivery pump, and the rectification reflux pump is provided with a branch and is connected with the top of the reflux buffer tank;
the top of the product rectifying tower is provided with a gas phase line and is connected with the negative pressure buffer tank, the vacuum pump set, the liquid phase enrichment tank and the liquid phase enrichment tank pump are sequentially connected through pipelines to form a recovery processing structure, and the bottom of the negative pressure buffer tank is also provided with a branch line and is connected with the liquid phase enrichment tank;
the product condenser lower part be provided with the discharging pipe and with the product delivery pump is connected, product delivery pump, product stabilization reaction kettle and product stabilization backwash pump loop through the pipe connection and form product secondary treatment output structure, the product stabilization backwash pump is provided with backward flow export and product outlet, the backward flow export of product stabilization backwash pump with the product stabilization reaction kettle is connected and is handled once more, the product outlet and the outside product tank district of product stabilization backwash pump are connected and output finished product.
Preferably, this device still is provided with remote control system, remote control system includes reaction control system, remote pump switch, remote valve switch and temperature pressure sensor, material transferring pump, distillation circulating pump, distillation residue pump, methyl alcohol backwash pump, n-hexane delivery pump, rectification backwash pump, product delivery pump, product stabilization backwash pump, vacuum pump group and liquid phase enrichment jar pump all are provided with remote pump switch, esterification reaction cauldron, catalyst ration injection pump, distillation reation kettle, catalyst stills, methyl alcohol distillation cooler, methyl alcohol backwash jar, n-hexane washing knockout drum, n-hexane intermediate tank, product rectification tower, product condenser, backward flow buffer tank, product stabilization reation kettle, negative pressure buffer tank and liquid phase enrichment jar all are provided with remote control valve and temperature pressure sensor, remote pump switch, remote control system, The remote valve switch and the temperature pressure sensor are respectively electrically connected with the reaction control system.
Compared with the prior art, the utility model, have following advantage:
1. the utility model adopts a plurality of double reactors for continuous reaction, and the design of feeding and discharging materials in sequence, thereby prolonging the reaction time, increasing the reaction depth and realizing the continuous production;
2. methanol distillation and product refining prevent reactants from polymerizing through low-oxygen air, and no polymerization inhibitor is added, so that the separation efficiency of intermediate products and byproducts is improved, and the running cost of the device is reduced;
3. the device adopts the DCS control system to carry out centralized management and remote dispersion accurate control on the production process, improves the production level and the product quality of enterprises, reduces the labor intensity of workers, and improves the automation level and the management level of the enterprises;
4. the catalyst adopts a catalyst quantitative injection pump to adjust the injection rate and the total amount of the catalyst, which is beneficial to controlling the whole reaction process to be carried out stably and ensuring the reaction yield and the product purity;
5. the packing design of the distillation cooler is optimized, the liquid phase and gas phase dynamics principle is fully utilized, the cooling effect is ensured, and the material separation efficiency is improved.
Drawings
Fig. 1 is a schematic structural view of the present invention;
in the figure: 1-an esterification reaction kettle, 2-a catalyst quantitative injection pump, 3-a reaction heater, 4-a transfer pump, 5-a distillation reaction kettle, 6-a distillation circulating pump, 7-a distillation cooler, 8-a distillation feed pump, 9-a catalyst distillation kettle, 10-a distillation residue pump, 11-a catalyst condenser, 12-a catalyst tank, 13-a methanol distillation tower, 14-a methanol distillation cooler, 15-a methanol reflux tank, 16-a methanol reflux pump, 17-a normal hexane water washing separation tank, 18-a normal hexane intermediate tank, a 19-a normal hexane delivery pump, 20-a product rectification tower, 21-a product condenser, 22-a reflux buffer tank, 23-a rectification reflux pump, 24-a product delivery pump and 25-a product stabilization reaction kettle, 26-a product stable reflux pump, 27-a negative pressure buffer tank, 28-a vacuum pump set, 29-a liquid phase enrichment tank, 30-a liquid phase enrichment tank pump, an A-esterification reaction unit, a B-distillation reaction unit, a C-catalyst recovery unit, a D-product rectification unit and an E-methanol and alkane distillation recovery unit.
Detailed Description
In the following description, numerous implementation details are set forth in order to provide a more thorough understanding of the present invention. It should be understood, however, that these implementation details should not be used to limit the invention. That is, in some embodiments of the invention, details of these implementations are not necessary. In addition, some conventional structures and components are shown in simplified schematic form in the drawings.
Example one
Referring to fig. 1, the device comprises an esterification reaction unit, a distillation reaction unit, a catalyst recovery unit, a methanol and alkane distillation recovery unit and a product rectification unit.
An esterification reaction unit: feeding methyl acrylate and dimethylethanolamine from the top of the esterification reaction kettle 1; feeding the catalyst from the top of the esterification reaction kettle 1 through a catalyst quantitative injection pump 2; a material outlet line at the top of the esterification reaction kettle 1 is connected with a material inlet line of the methanol distillation tower 13; a material outlet line at the bottom of the methanol distillation tower 13 feeds materials from the top of the esterification reaction kettle 1; feeding n-hexane from the top of the esterification reaction kettle 1 through an n-hexane delivery pump 19; a material outlet line at the bottom of the esterification reaction kettle 1, a material transferring pump 4 and a reaction heater 3 form an esterification reaction heating circulation closed circuit;
a distillation reaction unit: the esterification reaction kettle 1 is fed from the top of the distillation reaction kettle 5 through a reaction heating circulation closed-loop side discharge line; a material outlet line at the top of the distillation reaction kettle 5 is connected with a material inlet line of the product rectifying tower 20; a material outlet line at the bottom of the product rectifying tower 20 feeds materials from the top of the distillation reaction kettle 5; a material outlet line at the bottom of the distillation reaction kettle 5, a distillation circulating pump 6 and a distillation cooler 7 form a distillation reaction cooling circulation closed loop;
a catalyst recovery unit: a discharge branch line at the bottom of the catalyst distillation reaction kettle 5 feeds from the top of a catalyst distillation kettle 9 through a distillation material pumping pump 8; a material outlet line at the bottom of the catalyst distillation kettle 9 is divided into two parts by a distillation residue pump 10, the feeding is carried out at the top of the main catalyst distillation kettle 9 to form a circulation closed circuit, and the other part sends the distillation residue to a tank area; a material outlet line at the top of the catalyst distillation kettle 9 enters a catalyst tank 12 through a catalyst condenser 11 for reutilization;
methanol and alkane distillation recovery unit: a material line is ejected out of the esterification reaction kettle 1, and low-oxygen air enters the methanol distillation tower 13; the top gas phase line of the methanol distillation tower 13 enters a methanol distillation cooler 14 from the top; a discharge line at the bottom of the methanol distillation cooler 14 enters a methanol reflux tank 15 from the top; a discharge line at the bottom of the methanol reflux tank 15 is divided into two parts by a methanol reflux pump 16, a main line refluxes the methanol distillation tower 13, and a lateral line enters an n-hexane washing separation tank 17; deionized water enters the n-hexane washing separation tank 17 through a lateral line; a discharging line at the side of the normal hexane washing separation tank 17 enters a normal hexane intermediate tank 18; discharging from the bottom of the normal hexane washing separation tank 17 to be a methanol water tank removing area; a material outlet line at the bottom of the n-hexane intermediate tank 18 is divided into two parts by an n-hexane delivery pump 19, a main line reflows to the n-hexane intermediate tank 18, and a lateral line enters the esterification reaction kettle 1 from the top; the new n-hexane is supplemented by the tank field;
a product rectification unit: a material outlet line at the top of the distillation reaction kettle 5 and low-oxygen air enter a product rectifying tower 20; the gas phase on the top of the product rectifying tower 20 enters a product condenser 21; the low discharge line of the product condenser 21 enters a reflux buffer tank 22 from the top; a discharge line at the bottom of the reflux buffer tank 22 is divided into two parts by a rectification reflux pump 23, a main line is refluxed to the product rectifying tower 20, and a lateral line is refluxed to the reflux buffer tank 22; a material outlet line at the side of the reflux buffer tank 22 feeds materials from the top of a product stabilization reaction kettle 25 through a product conveying pump 24; a discharge line at the bottom of the product stabilization reaction kettle 25 is divided into two parts by a product stabilization reflux pump 26, a main line refluxes the product stabilization reaction kettle 25, and a side line qualified product is sent to a tank area; the top gas phase line of the product condenser 21 enters a negative pressure buffer tank 27; the liquid phase at the bottom of the negative pressure buffer tank 27 enters a liquid phase enrichment tank 29; the non-condensable gas in the negative pressure buffer tank 27 enters a liquid phase enrichment tank 29 through a vacuum pump set 28; the discharge line at the bottom of the liquid phase enrichment tank 29 is sent to the recovery tank through a liquid phase enrichment tank pump 30.
The process flow is as follows:
the esterification distillation reaction process flow comprises the following steps: adding quantitative methyl acrylate and dimethylethanolamine into an esterification reaction kettle 1 for esterification reaction, adding a catalyst through a catalyst quantitative injection pump 2, and adjusting the injection amount of the catalyst in real time according to the detection condition of the reaction process, wherein the reaction is endothermic, reaction materials enter a reaction heater 3 through a material transfer pump 4 for slow heating, the reaction pressure of the esterification reaction kettle 1 is designed to be normal pressure, the reaction temperature is 80-110 ℃, and the reaction time is 10-15 hours; feeding n-hexane from the top of the esterification reaction kettle 1 through an n-hexane delivery pump 19; the normal hexane makes the generated methanol and the normal hexane form an azeotrope, and the azeotrope enters a methanol distillation tower 6 for separation.
After the esterification reaction kettle 1 reaches the reaction set time, the reaction material enters a distillation reaction kettle 5 for continuous reaction, the reaction conditions refer to the esterification reaction kettle 1, and the reaction temperature is regulated by pumping the material into a distillation cooler 7 through a distillation circulating pump 6; the gas phase reactant enters a product rectifying tower 20 for rectification; after the index of the liquid phase reaction material reaches the specified requirement, pumping the liquid phase reaction material into a catalyst distillation kettle 9 through a distillation material pumping pump 8; the liquid phase of the catalyst distillation kettle 9 is internally circulated by a distillation residue pump 10 until the distillation sampling is qualified, and then the internal circulation is closed, and the liquid phase distillation residue is sent to a tank area; the gas phase catalyst distilled from the catalyst distillation kettle 9 is condensed by a catalyst condenser and then enters a catalyst tank for standby.
Methanol and alkane distillation recovery unit: feeding methanol and n-hexane gas-phase azeotrope and low-oxygen air in the esterification reaction kettle 1 into a methanol distillation tower 13; the operation temperature of the top of the methanol distillation tower 13 is 40-55 ℃, and the operation pressure is micro-positive pressure; the liquid phase reactant in the methanol distillation tower 13 flows back to the esterification reaction kettle 1 for re-reaction; cooling a gas phase of a methanol distillation tower 13 by a methanol distillation cooler 14, and then feeding a liquid phase into a methanol reflux tank 15, wherein the outlet temperature of the methanol distillation cooler 14 is kept at 0-4 ℃; the liquid phase of the methanol reflux tank 15 is divided into two parts by a methanol reflux pump 16, a main line refluxes the methanol distillation tower 13, and a lateral line enters an n-hexane washing separation tank 17; deionized water is added through a lateral line, and n-hexane is separated by washing and enters an n-hexane intermediate tank 18 for recycling; discharging from the bottom of the normal hexane washing separation tank 17 to be a methanol water tank removing area; a material outlet line at the bottom of the n-hexane intermediate tank 18 is divided into two parts by an n-hexane delivery pump 19, a main line reflows to the n-hexane intermediate tank 18, and a lateral line enters the esterification reaction kettle 1 from the top; new n-hexane is replenished from the tank field.
A product rectification unit: the gas-phase reactant and the low-oxygen air in the distillation reaction kettle 5 enter a product rectifying tower 20; the operation temperature of the top of the product rectifying tower 20 is 40-55 ℃, and the operation pressure is-170 to-300 mbar; the gas phase of the product in the product rectifying tower 20 enters a product condenser 21 for condensation, and the outlet temperature of the product condenser 21 is kept at-2 to 2 ℃; the condensed liquid phase enters a reflux buffer tank 22; the liquid phase of the reflux buffer tank 22 is divided into two parts by a rectification reflux pump 23, a main line is refluxed to the product rectifying tower 20, and a lateral line is refluxed to the reflux buffer tank 22; the product in the reflux buffer tank 22 is pumped into a product stabilization reaction kettle 25 through a product delivery pump 24; determining the reflux running time of the product stabilizing reflux pump 26 according to product indexes, wherein the designed reflux time range is 1-2 h, stopping reflux after the product indexes are qualified, and removing qualified products to a tank area through a lateral line of the product stabilizing reflux pump 26; the gas phase of the product condenser 21 enters a negative pressure buffer tank 27; the liquid phase at the bottom of the negative pressure buffer tank 27 enters a liquid phase enrichment tank 29; the noncondensable gas in the negative pressure buffer tank 27 is pumped into a liquid phase enrichment tank 29 through a vacuum pump unit 28; the liquid phase in the liquid phase enrichment tank 29 is sent to the recovery tank by the liquid phase enrichment tank pump 30.
The present invention is not limited to the above-described embodiments, and various changes can be made within the knowledge range of those skilled in the art without departing from the spirit of the present invention, and the changed contents still belong to the protection scope of the present invention.
Claims (6)
1. A production device for preparing a high molecular polymer intermediate through esterification reaction is characterized in that: the device comprises an esterification reaction unit, a distillation reaction unit, a catalyst recovery unit and a product rectification unit, wherein the esterification reaction unit is connected with the distillation reaction unit through a pipeline, the distillation reaction unit is provided with a gas phase line and a liquid phase line, the gas phase line is connected with the product rectification unit, the liquid phase line is connected with the catalyst recovery unit, the product rectification unit is provided with a discharge pipeline and is connected with an external product tank area to produce a finished product, and the catalyst recovery unit is provided with a discharge pipeline and is connected with an external catalyst recovery tank to recover a catalyst;
the esterification reaction unit comprises an esterification reaction kettle, a catalyst quantitative injection pump, a reaction heater and a material transferring pump, wherein the catalyst quantitative injection pump is connected with a feed inlet at the top of the esterification reaction kettle, the top of the esterification reaction kettle is also provided with a feed inlet for methyl acrylate, dimethylethanolamine and n-hexane, the bottom of the esterification reaction kettle is provided with a liquid phase pipeline and is connected with the material transferring pump, the material transferring pump is provided with a reflux outlet and a distillation outlet, the reaction heater is connected with the reflux outlet of the material transferring pump, the top of the reaction heater is connected with the top of the esterification reaction kettle, and the distillation reaction unit is connected with the distillation outlet of the material transferring pump.
2. The apparatus for producing a polymer intermediate by an esterification reaction according to claim 1, wherein: the top of the esterification reaction kettle is also connected with a methanol and alkane distillation recovery unit, and the methanol and alkane distillation recovery unit comprises a methanol distillation tower, a methanol distillation cooler, a methanol reflux tank, a methanol reflux pump, a n-hexane washing separation tank, a n-hexane intermediate tank and a n-hexane delivery pump;
the esterification reaction kettle, the methanol distillation tower, the methanol distillation cooler, the methanol reflux tank, the methanol reflux pump and the n-hexane washing separation tank are sequentially connected through a pipeline and enter the methanol distillation tower to form a methanol distillation recovery structure, the n-hexane washing separation tank is also provided with a deionized water feeding pipe, the lower part of the methanol distillation tower is also provided with a low-oxygen air feeding pipeline, and the middle part of the methanol distillation tower is provided with a pipeline and is connected with an external methanol water tank zone;
the esterification reaction kettle, the methanol distillation tower, the n-hexane intermediate tank and the n-hexane delivery pump are sequentially connected through pipelines and enter the esterification reaction kettle to form an alkane distillation recovery structure;
the methanol reflux pump is provided with a gas phase outlet and is connected with the methanol distillation tower, the n-hexane washing separation tank is provided with a liquidus and is connected with the n-hexane intermediate tank, and the n-hexane delivery pump is provided with a gas phase line and is connected with the n-hexane intermediate tank.
3. The apparatus for producing a polymer intermediate by an esterification reaction according to claim 1, wherein: the distillation reaction unit includes distillation reation kettle, distillation circulating pump and distillation cooler, the distillation reation kettle top be provided with the feed inlet and with the commentaries on classics material pump is connected, the distillation reation kettle lower part be provided with the liquid phase pipeline and with the distillation circulating pump is connected, the distillation circulating pump is provided with backward flow export and residue export, the distillation cooler with the backward flow exit linkage of distillation circulating pump, the distillation cooler with the distillation reation kettle is connected, catalyst recovery unit with the residue exit linkage of distillation circulating pump.
4. The apparatus for producing a polymer intermediate by an esterification reaction according to claim 3, wherein: the catalyst recovery unit includes distillation pump, catalyst stills, distillation residue pump, catalyst condenser and catalyst jar, distillation pump, catalyst stills, catalyst condenser and catalyst jar loop through the pipe connection, catalyst stills bottom with the distillation residue pump is connected, the distillation residue pump is provided with backflow outlet and residue export, the catalyst stills with the backflow outlet of distillation residue pump is connected and is formed the backward flow processing structure, the residue export of distillation residue pump is connected with outside distillation residue processing area and is discharged the residue.
5. The apparatus for producing a polymer intermediate by an esterification reaction according to claim 1, wherein: the product rectification unit comprises a product rectification tower, a product condenser, a reflux buffer tank, a rectification reflux pump, a product delivery pump, a product stabilization reaction kettle, a product stabilization reflux pump, a negative pressure buffer tank, a vacuum pump set, a liquid phase enrichment tank and a liquid phase enrichment tank pump, and a low-oxygen air pipeline is arranged at the lower part of the product distillation tower;
the distillation reaction kettle, the product rectifying tower, the product condenser, the reflux buffer tank and the rectifying reflux pump are sequentially connected through a pipeline and enter the distillation reaction kettle to form a product primary treatment circulating structure; the top of the product condenser is provided with a gas phase pipeline branch and is connected with the negative pressure buffer tank, the lower part of the reflux buffer tank is provided with a liquid phase pipeline branch and is connected with the product delivery pump, and the rectification reflux pump is provided with a branch and is connected with the top of the reflux buffer tank;
the top of the product rectifying tower is provided with a gas phase line and is connected with the negative pressure buffer tank, the vacuum pump set, the liquid phase enrichment tank and the liquid phase enrichment tank pump are sequentially connected through pipelines to form a recovery processing structure, and the bottom of the negative pressure buffer tank is also provided with a branch line and is connected with the liquid phase enrichment tank;
the product condenser lower part be provided with the discharging pipe and with the product delivery pump is connected, product delivery pump, product stabilization reaction kettle and product stabilization backwash pump loop through the pipe connection and form product secondary treatment output structure, the product stabilization backwash pump is provided with backward flow export and product outlet, the backward flow export of product stabilization backwash pump with the product stabilization reaction kettle is connected and is handled once more, the product outlet and the outside product tank district of product stabilization backwash pump are connected and output finished product.
6. The apparatus for producing a polymer intermediate by an esterification reaction according to claim 1, wherein: the device is also provided with a remote control system which comprises a reaction control system, a remote pump switch, a remote valve switch and a temperature pressure sensor, the material transferring pump, the distillation circulating pump, the distillation material pumping pump, the distillation residue pump, the methanol reflux pump, the normal hexane conveying pump, the rectification reflux pump, the product conveying pump, the product stabilizing reflux pump, the vacuum pump set and the liquid phase enrichment tank pump are all provided with remote pump switches, the esterification reaction kettle, the catalyst quantitative injection pump, the distillation reaction kettle, the catalyst distillation kettle, the methanol distillation cooler, the methanol reflux tank, the n-hexane water washing separation tank, the n-hexane intermediate tank, the product rectifying tower, the product condenser, the reflux buffer tank, the product stabilization reaction kettle, the negative pressure buffer tank and the liquid phase enrichment tank are all provided with a remote control valve and a temperature pressure sensor, the remote pump switch, the remote valve switch and the temperature pressure sensor are respectively electrically connected with the reaction control system.
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| CN202120661198.3U CN214973960U (en) | 2021-04-01 | 2021-04-01 | Production device for preparing high-molecular polymer intermediate through esterification reaction |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114685294A (en) * | 2022-04-29 | 2022-07-01 | 山东蓝湾新材料有限公司 | Rectification separation method of dimethylaminoethyl acrylate and dimethylaminoethyl methacrylate |
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2021
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114685294A (en) * | 2022-04-29 | 2022-07-01 | 山东蓝湾新材料有限公司 | Rectification separation method of dimethylaminoethyl acrylate and dimethylaminoethyl methacrylate |
| CN114685294B (en) * | 2022-04-29 | 2024-01-26 | 山东蓝湾新材料有限公司 | Rectification separation method of dimethylaminoethyl acrylate and dimethylaminoethyl methacrylate |
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