CN211358850U

CN211358850U - Continuous energy-saving production device for acrylic polymer

Info

Publication number: CN211358850U
Application number: CN201921605179.8U
Authority: CN
Inventors: 刘振华; 张涌; 陈胜环
Original assignee: Sichuan Flower's Song Fine Chemical Co ltd
Current assignee: Sichuan Flower's Song Fine Chemical Co ltd
Priority date: 2019-09-25
Filing date: 2019-09-25
Publication date: 2020-08-28
Anticipated expiration: 2029-09-25

Abstract

The utility model discloses an energy-conserving apparatus for producing of acrylic polymer serialization, include: steam injection reactors and pipeline reactors; the steam jet reactor comprises a steam jet reactor main body, a steam generator and a feeding pipe group; the pipeline reactor comprises a steam condensation reflux pipe, a steam condenser and a polymerization reaction condenser; and cooling water outlets of the steam condenser and the polymerization reaction condenser are connected with the steam generator through process pipelines. The advantages are that: the heat generated by each stage of the equipment is fully utilized to supply heat to the steam generator, and the production energy consumption is greatly reduced.

Description

Continuous energy-saving production device for acrylic polymer

Technical Field

The utility model relates to a polymerization reaction device, in particular to a production device for acrylic polymers.

Background

The acrylic polymer mentioned in the industry mainly refers to polyacrylic acid homopolymer polymerized from acrylic acid, or copolymer polymerized from acrylic acid and other raw materials, such as maleic copolymer copolymerized from maleic acid and acrylic acid, and also includes sodium salt, such as sodium polyacrylate, etc. formed by neutralizing with alkaline agent, such as sodium hydroxide.

It is well known in the art that the difference in molecular weight of acrylic polymers has a significant effect on the application properties thereof, and therefore, the production of acrylic polymers of different molecular weight sizes and different molecular weight distribution ranges for different uses of acrylic polymers is an important subject of research in the art.

At present, a production device of an acrylic polymer mainly adopts a polymerization reaction kettle, and the production mode is that raw materials such as a monomer, an initiator, a chain transfer agent and the like are added into the reaction kettle and react at a proper temperature for a proper reaction time to obtain a product. In the scheme, although the molecular weight distribution of the product can be controlled to a certain extent by factors such as the type and proportion of the initiator, the type and amount of the chain transfer agent, the reaction temperature, the monomer concentration, the stirring speed, the feeding program, the feeding speed and the like, the method is limited by the full mixing characteristic of the tank reactor, the material backmixing is serious, and the product with narrow molecular weight distribution is difficult to obtain. On the other hand, the polymerization reaction kettle needs to be fed in batches, only batch production can be carried out, which easily causes inconsistent product quality of each batch and influences sale and use. And thirdly, in the production of the kettle type reactor, because the polymerization heat of the monomers is large and the closed reaction is carried out, the implosion is easy to occur, and the potential safety hazard is great.

In order to solve the above problems, a tubular reactor is proposed to replace a kettle reactor, so as to better solve the problem of material back mixing, obtain a product with narrow molecular weight distribution, simultaneously realize continuous reaction and normal pressure reaction, and simultaneously solve the problems of product quality fluctuation and implosion, but the tubular reactor still has the defects:

1. the tubular reactor is theoretically a plug flow reactor, but actually, because the polymer has viscosity, the dragging effect of the retention layer on the tube wall is greatly influenced, and the production of the acrylic polymer needs long-time polymerization to be completed, so that the reaction time is long, the tube length is long, and the back mixing caused by the dragging effect of the retention layer in the tube cannot be easily considered.

2. The polymerization reaction heat effect of the acrylic acid is large, if the reaction temperature is high, the reaction speed is high, a reaction high-temperature area exists, and the product is discolored due to the existence of the high-temperature area; on the other hand, if the reaction temperature is low, the reaction time is long, and a long line is required, which makes industrial implementation difficult.

To solve the above problems, patent document CN104277142A discloses a method for producing a narrow distribution low molecular weight polymer, which comprises setting a steam jet reactor to rapidly polymerize monomers in the reactor, so that most of the polymerization reaction is completed in the steam jet reactor, thereby significantly reducing the reaction time of materials in a pipeline reactor, improving the back-mixing phenomenon, and obtaining a product with low molecular weight and a narrower molecular weight distribution range. However, this solution still has drawbacks:

firstly, the scheme needs to consume a large amount of high-temperature steam to heat the reaction materials, so that the energy consumption is high and the production cost is relatively high.

Secondly, as described above, there are different requirements for the molecular weight and molecular weight distribution of the product depending on the use of the acrylic polymer. Although the solutions of the above patent documents can obtain polymers having narrow molecular weights, it is difficult to adjust the molecular weight of the product and the molecular weight distribution range in production. Therefore, depending on the use of the product, when it is desired to produce a polymer product having a high molecular weight or a polymer product having a wide molecular weight distribution in a special case, the apparatus cannot be satisfied, only the production apparatus can be replaced, and the production apparatus is large in investment and very troublesome.

Further, in general, an industrially desired target product may be an acrylate polymer such as sodium polyacrylate, but the apparatus cannot directly obtain an acrylate polymer product, and therefore, if an acrylate polymer is to be produced, the obtained acrylate polymer must be separately passed into a neutralization reaction vessel for further neutralization production, which is not only large in equipment investment but also inconvenient for continuous and automated production, which is very troublesome.

SUMMERY OF THE UTILITY MODEL

For the production energy consumption that reduces acrylic polymer, reduction in production cost, the utility model provides an acrylic polymer serialization energy-conserving apparatus for producing.

The utility model provides a technical scheme that its technical problem adopted is: an energy-saving continuous production device for acrylic polymers, comprising:

a steam injection reactor;

the pipeline reactor is vertically arranged and is connected with a material outlet of the steam jet reactor;

the steam injection reactor comprises:

a steam injection reactor body;

the steam generator is connected with the steam jet reactor main body through a steam pipeline;

a feed tube bank for feeding the steam injection reactor body;

the pipeline reactor comprises:

a steam condensing reflux pipe for condensing reflux steam;

the steam condenser is a water-cooled condenser, is arranged on the steam condensation return pipe and is used for absorbing the heat released by the steam flowing through the steam condensation return pipe;

the polymerization reaction condenser is a water-cooled condenser, is arranged on the pipeline reactor and is used for absorbing the heat generated by the polymerization reaction;

a cooling water outlet of the polymerization reaction condenser is connected with a cooling water inlet of the steam condenser through a process pipeline; and a cooling water outlet of the steam condenser is connected with the steam generator through a process pipeline.

This scheme is through setting up steam condenser and polymerization ware and come continuous absorption steam condensation heat and the polymerization heat of giving off through same deionized cooling water, the cooling water that is used for the heat transfer after the heat absorption is heated, the temperature risees, then the cooling water after will being heated inserts steam generator as steam raw materials, heat energy and the polymerization heat of giving off that fully recycle steam produced heat energy and steam heating, greatly reduced the outside energy consumption that is used for heating steam, reach reduction in production cost's purpose.

As a further improvement of the present invention, the pipeline reactor further comprises:

the upper end pipeline, the circuitous pipeline and the lower end pipeline are sequentially arranged along the material flow direction;

the molecular weight adjusting pipeline and a first valve for opening and closing the molecular weight adjusting pipeline; when the first valve is opened, the material in the pipeline reactor can enter the lower end pipeline from the molecular weight regulating pipeline, so that the stroke of the material in the circuitous pipeline is reduced.

The device may be used as follows:

(1) when a high molecular weight product needs to be produced, the first valve is closed, the material enters the pipeline reactor after being rapidly reacted by the steam jet reactor, and flows through the upper end pipeline, the circuitous pipeline and the lower end pipeline in the pipeline reactor in sequence to complete the reaction, and the product is obtained after discharging. Since the material is still at its reaction temperature, which is relatively high when flowing through the circuitous conduit, the circuitous conduit increases the reaction time of the material at the appropriate temperature to promote more polymerization of the acrylic acid and thereby form a higher molecular weight polymer. The method is easy to obtain the product with the molecular weight distribution range of 7000-20000.

(2) When a low molecular weight product needs to be produced, the first valve is opened, so that the material directly enters the lower end pipeline from the molecular weight adjusting pipeline, and does not pass through a subsequent roundabout segment, so that a product with a higher molecular weight cannot be polymerized, and the obtained product is a low molecular weight product. The method is easy to obtain products with the molecular weight distribution range of 1000-7000.

(3) When a product with a wide molecular weight distribution range needs to be produced under special conditions, a part of materials can directly enter the lower end pipeline from the molecular weight adjusting pipeline by adjusting the opening degree of the first valve and matching the feeding speed, and the other part of materials still need to pass through all roundabout pipelines, so that the product with the molecular weight distribution range of 1000-20000 can be obtained.

It is easy to understand that the upper end pipeline, the circuitous pipeline and the lower end pipeline can be integrally formed to form the pipeline reactor, and can also be detachably connected to form the pipeline reactor, preferably detachably connected to facilitate the cleaning, maintenance and transfer of equipment.

The circuitous pipes can be coiled pipes, and besides the coiled pipes, other circuitous pipe forms which are common in the field, such as annular circuitous pipes and the like, can also be adopted.

More preferably, the serpentine pipe is roundabout up and down on a vertical plane and comprises n roundabout parts, and n is an even number which is greater than or equal to 2. Therefore, the opening of the material outlet end of the coiled pipe is downward, the material can flow in the pipeline reactor conveniently, and the arrangement of the molecular weight adjusting pipeline is convenient.

Preferably, a roundabout part of the serpentine pipe close to the upper end pipeline is a first roundabout part, and the first roundabout part is provided with a second valve for discharging materials in the first roundabout part. Because the steam pressure generated by the steam generator must be ensured to be stable before the reaction is carried out in the steam jet reactor, the steam pressure needs to be adjusted before the reaction, and the reaction is carried out after the steam pressure is stable. During this period, the condensed water produced by the steam is collected in the first detour part of the coiled pipe, and the condensed water can be discharged through the second valve. In addition, the second valve has another function of facilitating the sampling control in the reaction.

The utility model provides a concrete arrangement of molecular weight regulation pipeline, as shown in FIG. 2, when the coiled pipe circuitous about on vertical plane and had 2 circuitous portions, the molecular weight regulation pipeline communicates between the material exit end of first circuitous portion and lower extreme pipeline. When the first valve is opened, the material will enter the back end pipeline from the molecular weight regulating pipeline. As can be seen from fig. 3, the material outlet end of the first roundabout portion of the present invention means that the material leaves the end of the first roundabout portion when flowing through the first roundabout portion.

the neutralization reagent feeding pipe is communicated with the lower end pipeline;

the neutralization control valve is used for opening and closing the neutralization reagent feeding pipe;

and the neutralizing filler column is arranged in the pipeline reactor at the downstream of the neutralizing reagent feeding pipe in the material flowing direction, and the filler of the neutralizing filler column is a ceramic filler with the diameter of 20-40 mm.

In the scheme, the inventor proposes a technical idea of carrying out neutralization reaction in a pipeline reactor, but because the residence time of materials in a pipeline is short and the materials are difficult to be fully mixed with a neutralizing reagent, the inventor proposes to arrange a neutralizing filler column in the pipeline reactor, wherein the filler of the neutralizing filler column is ceramic filler with the diameter of 20-40 mm. When the neutralization reagent and the materials pass through the neutralization packing column, the contact time and the contact area of the materials and the neutralization reagent are increased by the packing column, so that the materials are fully mixed in the pipeline reactor, and the neutralization reaction is completed. The filler used by the neutralization filler column is a ceramic filler with the diameter of 20-40 mm, if the diameter is too low, the filler amount is increased, the compactness is increased, the resistance of liquid flow is increased, the polymer cannot be discharged smoothly, if the diameter is too large, the neutralization reagent and the polymer are neutralized unevenly, and the pH is locally too high or too low.

The utility model discloses the realization adopts same device can be used for producing acrylic acid polymer, also can be used for producing acrylate polymer, as shown in figure 2, only need when needing to produce acrylic acid polymer to close the valve with the neutralization can. And the device can realize the continuous production of the acrylate polymer.

As a further improvement of the utility model, still include pH monitoring devices, pH monitoring devices sets up on the pipeline reactor along the neutralization packing post low reaches of material flow direction for the pH of the material of monitoring flowing through. The scheme can realize the measurement of an on-line pH meter through the pH monitoring device, and can adjust the adding speed of the liquid caustic soda in real time by monitoring the pH value of a finished product.

As a further improvement of the utility model, the system further comprises a neutralization reaction condenser which is arranged on the pipeline reactor and used for absorbing the heat released in the neutralization reaction, wherein the neutralization reaction condenser is a water-cooled condenser, and the cooling water outlet of the neutralization reaction condenser is connected with the cooling water inlet of the polymerization reaction condenser through a process pipeline. This scheme absorbs the neutralization reaction through setting up neutralization reaction condenser and releases heat, the cooling water is heated after the heat absorption, because the use is same cooling water, the cooling water after being heated gets into polymerization reaction condenser and steam condenser again in proper order and continues the heat absorption, the cooling water that makes finally get into steam generator has fully absorbed the heat production of reacting each stage, possess higher temperature, the leading-in steam generator of cooling water after will being heated again, it is exothermic with each stage of full recovery reaction, further reduce steam generator energy consumption. The scheme can provide a large amount of heat sources for the steam generator, and the energy consumption of the steam generator is obviously reduced.

As a further improvement of the utility model, the cooling medium used by each condenser is deionized water. This is because the cooling medium of the condenser in the utility model finally enters the steam generator to generate high temperature steam to participate in the reaction, and is condensed into liquid by the steam condensing reflux pipe to directly enter the product to serve as a solvent for adjusting the solid content of the product. Therefore, to avoid introducing impurities into the product, deionized water should be used as the cooling medium for the condenser. In addition, the deionized water is used as a cooling medium, so that the service life of the equipment is prolonged to a certain extent, and the deionized water hardly contains impurities such as calcium ions, magnesium ions and the like, so that the loss degree of the equipment is reduced to the minimum.

The utility model has the advantages that: 1) the heat generated by each stage of the equipment is fully utilized to supply heat to the steam generator, and the production energy consumption is greatly reduced. 2) The method can produce acrylic polymer and acrylate polymer by using the same production device, and can realize continuous neutralization production of the acrylate polymer. 3) The equipment has simple structure and convenient control, and the production and neutralization of the polymer are continuously finished in the same pipeline reactor, thereby being beneficial to realizing automatic production. 4) The production of acrylic polymer products with different molecular weights and different molecular weight distribution ranges can be realized by adopting the same production device, and the equipment investment and the land occupation investment are greatly reduced.

Drawings

Fig. 1 is a schematic structural diagram of an apparatus according to the first embodiment.

Fig. 2 is a schematic structural diagram of the apparatus according to the second embodiment.

FIG. 3 is a schematic view of a first detour structure.

Labeled as: 101-steam jet reactor body, 102-steam generator, 103-feeding pipe group, 2-pipeline reactor, 201-upper pipeline, 202-circuitous pipeline, 203-lower pipeline, 204-steam condensation return pipe, 205-molecular weight adjusting pipeline, 206-first valve, 207-second valve, 208-third valve, 209-neutralization reagent feeding pipe; 210-neutralization control valve, 211-neutralization packing column, 212-pH monitoring device, 213-discharge valve, 214-steam condenser, 215-polymerization condenser, 216-neutralization condenser.

Detailed Description

The present invention will be further explained with reference to the drawings and examples.

The first embodiment is as follows:

as shown in figure 1, the continuous energy-saving production device for acrylic polymer of the utility model comprises a steam jet reactor and a pipeline reactor 2, wherein the pipeline reactor 2 is vertically arranged and is connected with a material outlet of the steam jet reactor; the steam injection reactor comprises a steam injection reactor body 101; a steam generator 102 connected to the steam jet reactor main body 101 through a steam pipe; a feed tube group 103 for feeding the steam jet reactor main body 101. The pipe reactor 2 comprises a steam condensate return pipe 204 for condensing return steam; a steam condenser 214 disposed on the steam condensate return pipe 204 for absorbing heat released from the steam flowing through the steam condensate return pipe 204; a polymerization condenser 215 disposed on the pipe reactor 2 for absorbing exothermic heat of polymerization; the steam condenser 214 and the polymerization condenser 215 are water-cooled condensers. The cooling water outlet of the polymerization condenser 215 is connected with the cooling water inlet of the steam condenser 214 through a process pipeline; the cooling water outlet of the steam condenser 214 is connected with the steam generator 102 through a process pipe; the cooling water used in each condenser was deionized water.

When the steam generator works, the steam generator 102 is firstly opened, and the size of steam is adjusted according to the output, wherein the size of the steam is generally 0.1-0.4 MPa. After the steam is stabilized, acrylic acid, an initiator and a chain transfer agent are introduced into the steam jet reactor main body 101 through the feeding pipe group 103 at a constant speed, and the feeding speed is adjusted according to production requirements. Under the spraying action of high-temperature steam, the material is instantly atomized and heated by the steam, most of the reaction is completed within a few seconds, and the steam entering the pipeline reactor is condensed into deionized water by the steam condensing and returning pipe in the process and enters the product to play a role in adjusting the solid content of the product. The material then enters the pipeline reactor 2 for continuous reaction.

In the process, heat emitted in the polymerization reaction process is absorbed by the polymerization reaction condenser 215, cooling water after heat absorption enters the steam condenser 214 through a process pipeline, the heat emitted by high-temperature steam is continuously absorbed by the steam condenser 214, the temperature of the cooling water is obviously increased through continuous heat absorption, and the cooling water with higher temperature is introduced into the steam generator 102 to serve as a steam raw material, so that the energy consumption of the steam generator is reduced.

Example two:

as shown in fig. 2, the continuous energy-saving production apparatus for acrylic polymer in this embodiment has the following additional structure in addition to the structure in the first embodiment:

the pipeline reactor 2 further comprises: an upper end pipeline 201, a circuitous pipeline 202 and a lower end pipeline 203 which are arranged in sequence along the material flow direction; further comprises a molecular weight adjusting pipeline 205 and a first valve 206 for opening and closing the molecular weight adjusting pipeline 205; when the first valve 206 is opened, the material in the pipe reactor 2 can enter the lower end pipe 203 from the molecular weight adjusting pipe 205, thereby reducing the stroke of the material in the detour pipe 202.

The circuitous pipeline 202 is a coiled pipe, the coiled pipe is circuitous up and down on a vertical plane, and comprises 2 circuitous parts; a circuitous part of the coiled pipe close to the upper end pipeline 201 is a first circuitous part, and the first circuitous part is provided with a second valve 207 for discharging materials in the first circuitous part; the molecular weight regulating pipe 205 is communicated between the material outlet end of the first detour portion and the lower end pipe 203.

In addition to this, the pipeline reactor 2 further comprises: a neutralization reagent feeding pipe 209 communicated with the lower end pipeline and a neutralization control valve 210 for opening and closing the neutralization reagent feeding pipe 209; a column of neutralizing fillers 211 arranged inside the pipe reactor 2 downstream of the feeding pipe 209 for neutralizing agents in the direction of flow of the material, the filler of the column of neutralizing fillers 211 being a ceramic ring with a diameter of 30 mm. The pipeline reactor 2 further comprises a pH monitoring device 212, wherein the pH monitoring device 212 is arranged on the pipeline reactor 2 downstream of the neutralization packing column 211 along the material flowing direction and is used for monitoring the pH of the material flowing through. And a neutralization reaction condenser 216 arranged on the pipeline reactor 2 and used for absorbing the exothermic heat of the neutralization reaction, wherein the neutralization reaction condenser 216 is a water-cooled condenser, and a cooling water outlet of the neutralization reaction condenser 216 is connected with a cooling water inlet of the polymerization reaction condenser 215 through a process pipeline.

Besides all the advantages of the first embodiment, the solution has the following significant features:

firstly, absorb neutralization reaction through setting up neutralization reaction condenser 216 and release heat, the cooling water is heated after the heat absorption, the temperature rises, the cooling water is heated after the heat absorption, because the same cooling water that uses, the cooling water after being heated gets into polymerization reaction condenser and steam condenser again in proper order and continues the heat absorption, make the cooling water that finally gets into steam generator have fully absorbed the heat production of each stage of reaction, possess higher temperature, the cooling water after will heating is introduced into steam generator again, with the heat release of each stage of full recovery reaction, further reduce steam generator energy consumption. The scheme can provide a large amount of heat sources for the steam generator, and the energy consumption of the steam generator is obviously reduced.

Secondly, the production of acrylic polymer products with different molecular weights and different molecular weight distribution ranges can be realized by adopting the same production device, and the using method is as follows:

during operation, according to the production requirement, if the low molecular weight product is produced and the molecular weight is less than 7000, the first valve 206 is fully opened, and if the product with the molecular weight of 7000-20000 is produced, the first valve 206 is closed. And then, opening the steam generator 102, adjusting the steam pressure according to the yield, wherein the steam pressure is generally 0.1-0.4 MPa, and discharging condensed water for adjusting the steam through a second valve 207 after the steam is stabilized. Then, acrylic acid, an initiator and a chain transfer agent are fed into the reactor through a feeding pipe group 103 at a constant speed, and the feeding speed is adjusted according to production requirements. Under the spraying action of high-temperature steam, the material is instantly atomized and heated by the steam, most of the reaction is completed within a few seconds, and the steam entering the pipeline reactor is condensed into deionized water by the steam condensing and returning pipe in the process and enters the product to play a role in adjusting the solid content of the product. The material then enters the pipeline reactor 2 for continuous reaction, and products with different molecular weights and different molecular weight distribution ranges can be obtained in the pipeline reactor 2 by controlling the opening and closing of the first valve 206. Finally, through the sampling central control of the second valve 207, after the product is qualified, the third valve 208 is opened according to the type of the required product, so that the material enters a continuous neutralization section or the discharge valve 213 is directly opened to obtain the product.

Thirdly, continuous neutralization production can be realized, and the using method comprises the following steps:

when the neutralization control valve 210 is opened, the neutralization control valve 210 is closed, the steam generator 102 is opened, and the steam is adjusted according to the output, wherein the steam is generally 0.1-0.4 MPa. After the steam is stabilized, acrylic acid, an initiator and a chain transfer agent are introduced into the steam jet reactor main body 101 through the feeding pipe group 103 at a constant speed, and the feeding speed is adjusted according to production requirements. Under the action of the steam, the material is instantaneously atomized and heated by the steam, most of the reaction is completed within a few seconds, and then the material enters the pipeline reactor 2 for continuous reaction. After the reaction product is qualified by sampling, the third valve 208 is opened, the neutralization control valve 210 is opened at the same time, the liquid caustic soda enters the pipeline reactor 2 through the neutralization reagent feeding pipe 209, when the liquid caustic soda flows through the neutralization filler column 211, the polyacrylic acid and the sodium hydroxide are fully contacted under the action of the neutralization filler column 211 to obtain a sodium polyacrylate product, the measurement of an online pH meter can be realized through the pH monitoring device 212, and the adding speed of the liquid caustic soda can be adjusted in real time through monitoring the pH value of a finished product. Finally, the waste water is discharged through a discharge valve 213, and the whole process is continuously operated. When the acrylate polymer is not required to be produced, the neutralization control valve 210 is closed all the time during production, and the third valve 208 is opened.

Claims

1. An energy-saving continuous production device for acrylic polymers, comprising:

a steam injection reactor;

characterized in that the steam injection reactor comprises:

a steam injection reactor body;

a feed tube bank for feeding the steam injection reactor body;

the pipeline reactor comprises:

a steam condensing reflux pipe for condensing reflux steam;

2. The continuous energy-saving production apparatus for acrylic polymer according to claim 1, characterized in that:

the pipeline reactor further comprises:

3. The continuous energy-saving production apparatus for acrylic polymer according to claim 2, characterized in that: the circuitous pipeline is a coiled pipe.

4. The acrylic polymer continuous energy-saving production apparatus according to claim 3, characterized in that: the serpentine pipe is roundabout up and down on a vertical plane and comprises n roundabout parts, wherein n is an even number which is greater than or equal to 2.

5. The acrylic polymer continuous energy-saving production apparatus according to claim 4, characterized in that: the tortuous portion that the coiled pipe is close to upper end pipeline is first tortuous portion, first tortuous portion is provided with the second valve that is used for discharging the material in first tortuous portion.

6. The acrylic polymer continuous energy-saving production apparatus according to claim 5, characterized in that: the coiled pipe is provided with 2 circuitous parts, and the molecular weight adjusting pipeline is communicated between the material outlet end of the first circuitous part and the lower end pipeline.

7. The continuous energy-saving production apparatus for acrylic polymers according to any one of claims 2 to 6, characterized in that: the pipeline reactor further comprises:

8. The acrylic polymer continuous energy-saving production apparatus according to claim 7, characterized in that: the pipeline reactor also comprises a pH monitoring device which is arranged on the pipeline reactor at the downstream of the neutralization packed column along the material flowing direction and is used for monitoring the pH of the materials flowing through.

9. The acrylic polymer continuous energy-saving production apparatus according to claim 7, characterized in that: the system also comprises a neutralization reaction condenser which is arranged on the pipeline reactor and used for absorbing the heat released by the neutralization reaction, wherein the neutralization reaction condenser is a water-cooled condenser, and a cooling water outlet of the neutralization reaction condenser is connected with a cooling water inlet of the polymerization reaction condenser through a process pipeline.

10. The continuous energy-saving production apparatus for acrylic polymers according to any one of claims 1 to 6, 8 and 9, wherein: the cooling medium used in each condenser was deionized water.