CN112010998A

CN112010998A - Preparation process of modified carboxylic styrene-butadiene latex

Info

Publication number: CN112010998A
Application number: CN202011190486.1A
Authority: CN
Inventors: 李江年
Original assignee: Jiangxi Yeli Medical Instrument Co ltd
Current assignee: Jiangxi Yeli Medical Instrument Co ltd
Priority date: 2020-10-30
Filing date: 2020-10-30
Publication date: 2020-12-01

Abstract

The invention relates to a preparation process of modified carboxylic styrene-butadiene latex, which comprises the following steps: adding carboxylic styrene-butadiene latex into a reactor through a first feed opening, and adding a modifier into the reactor through a second feed opening to form a first polymer; adding an aqueous solution into the reactor through a third feed opening to perform a polymerization reaction to form a second polymer; thirdly, evaporating water vapor from the second polymer through a degassing container to form a third polymer; step four, packing and discharging the third polymer through a batch mixing container; at a certain reaction moment, the measured value of the latex viscosity is compared with a preset value, the first polymer and the intermediate polymer are made to accord with the preset condition by adjusting the stirring speeds of the first stirrer and the second stirrer and the size of the stirring paddle, the preparation process is simple, the reaction efficiency is further improved, and the labor cost of a complex process is saved.

Description

Preparation process of modified carboxylic styrene-butadiene latex

Technical Field

The invention relates to the field of polymers, in particular to a preparation process of modified carboxylic styrene-butadiene latex.

Background

The carboxylic styrene-butadiene latex is a milky water dispersion which is a copolymer generated by emulsion polymerization of butadiene, styrene and a small amount of carboxylic acid and other auxiliary agents, and the liquid has different gloss due to the influence on the light refractive index caused by different particle sizes. The carboxylic styrene-butadiene latex has the advantages of higher adhesive force and conjunctival strength, good mechanical and chemical stability, good fluidity and storage stability, large filling amount and the like. The modified carboxylic styrene-butadiene latex is a polymer generated by polymerization reaction of carboxylic styrene-butadiene latex and a modifier, and has excellent comprehensive performance compared with common carboxylic styrene-butadiene latex.

At present, some preparation processes of modified carboxylic styrene-butadiene latex are available, and the added modifier is mainly optimized, so that the comprehensive performance of the prepared modified carboxylic styrene-butadiene latex is improved, but the reaction efficiency is low, the preparation process is complex, errors are easy to occur, and the labor cost is high.

Disclosure of Invention

Therefore, the invention provides a preparation process of modified carboxylic styrene-butadiene latex, which can effectively solve the technical problems in the prior art.

In order to achieve the above object, the present invention provides a process for preparing a modified carboxylated styrene-butadiene latex, comprising:

adding carboxylic styrene-butadiene latex into a reactor through a first feed opening, adding a modifier into the reactor through a second feed opening, uniformly mixing by using a first stirrer to form a first polymer, detecting the bubble density of the first polymer in real time by using a bubble density detector, wherein the detected real-time bubble density is alpha, and detecting the concentration of the first polymer in real time by using a concentration detector, wherein the detected real-time concentration is beta;

adding an aqueous solution into a reactor through a third feed opening, uniformly mixing by using a second stirrer to form an intermediate polymer, adjusting a first temperature regulator to enable the aqueous solution and the first polymer to generate a polymerization reaction to form a second polymer, measuring the conversion rate of the polymerization reaction in real time by using a conversion rate measuring instrument, wherein the measured conversion rate is eta, measuring the polymerization reaction rate in real time by using a polymerization reaction rate measuring instrument, the measured polymerization reaction rate is R, measuring the latex viscosity of the second polymer in real time by using a viscosity measuring instrument, the measured latex viscosity is mu, and measuring the hydrogen ion concentration index of the second polymer in real time by using an acidity measuring instrument, wherein the measured hydrogen ion concentration index is P;

thirdly, evaporating water vapor of the second polymer through a degassing container to form a third polymer, and measuring the water content of the third polymer in real time by using a water content measuring instrument, wherein the measured water content is Q;

step four, packing and discharging the third polymer through a batch mixing container;

the reactor and the degassing container are connected with a central control module through wireless, the central control module is used for controlling the reaction process from the first step to the third step, and a matrix is arranged in the central control module;

the first stirrer is provided with a first stirring regulator for regulating the stirring speed of the first stirrer and the size of the stirring paddle of the first stirrer;

the central control module is provided with a preset bubble density matrix alpha 0 (alpha 01, alpha 02, alpha 03, …, alpha 0 n), alpha 01 < alpha 02 < alpha 03 < … < alpha 0n, wherein alpha 01 represents a first preset bubble density, alpha 02 represents a second preset bubble density, alpha 03 represents a third preset bubble density, … and alpha 0n nth preset bubble density;

the central control module is also provided with a stirring speed matrix Va (Va 1, Va2, Va 3), wherein Va1 represents a first stirring speed of the first stirrer, Va2 represents a second stirring speed of the first stirrer, and Va3 represents a third stirring speed of the first stirrer;

the central control module is also provided with a stirring paddle matrix Ba (Ba 1, Ba 2), the Ba1 represents a small stirring paddle of the first stirrer, and the Ba2 represents a large stirring paddle of the first stirrer;

the central control module is further provided with a preset concentration range matrix beta 0 (beta 01, beta 02, beta 03), wherein beta 01 is larger than beta 02 and smaller than beta 03, wherein beta 01 represents a first preset concentration range, beta 02 is a second preset concentration range, and beta 03 represents a third preset concentration range;

the second stirrer is provided with a second stirring regulator for regulating the stirring speed of the second stirrer and the size of the stirring paddle of the second stirrer;

the central control module is also provided with a stirring speed matrix Vb (Vb 1, Vb 2), wherein Vb1 represents the first stirring speed of the second stirrer, and Vb2 represents the second stirring speed of the second stirrer;

the central control module is also provided with a stirring paddle matrix Bb (Bb 1, Bb 2), wherein Bb1 represents a small stirring paddle of the second stirrer, and Bb2 represents a large stirring paddle of the second stirrer;

the second stirrer is provided with a preset length L, a density detector is arranged on the second stirrer, the density detector can detect real-time densities at different positions of the second stirrer in the vertical direction, wherein the uppermost first density detection point is set to obtain a first density matrix rho 1i at different moments, the middle second density detection point is set to obtain a second density matrix rho 2i at different moments, the lowermost third density detection point is set to obtain a third density matrix rho 3i at different moments, a density matrix rho 0 (rho 1i, rho 2i, rho 3 i) of the middle polymer is formed, and the real-time average density rho of the middle polymer is calculated according to the following calculation formula:

where ρ 1i represents a first density matrix, ρ 2i represents a second density matrix, and ρ 3i represents a third density matrix;

the density detector is internally provided with a control unit which is a PLC control panel, and an intermediate polymer preset average density matrix rho a (rho 11, rho 12, rho 13) is arranged in the PLC control panel, wherein rho 11 represents a first intermediate polymer preset average density range, rho 12 represents a second intermediate polymer preset average density range, and rho 13 represents a third intermediate polymer preset average density range;

if the real-time bubble density alpha is less than a first preset bubble density alpha 01, controlling the first stirring regulator to enable the stirring speed to be a first stirring speed Va1 of the first stirrer;

if the real-time bubble density alpha is larger than the nth preset bubble density alpha 0n, controlling the first stirring regulator to enable the stirring speed to be the third stirring speed Va3 of the first stirrer;

if the first preset bubble density alpha 01 is not more than the real-time bubble density alpha 0n, controlling the first stirring regulator to enable the stirring speed to be the second stirring speed Va2 of the first stirrer, obtaining a value of a real-time concentration beta, if the real-time concentration beta is within the first preset concentration range beta 01, controlling the first stirring regulator to enable the stirring paddle to be a large stirring paddle Ba2 of the first stirrer, if the real-time concentration beta is within the second preset concentration range beta 02, controlling the first stirring regulator to enable the stirring paddle to be a small stirring paddle Ba1 of the first stirrer, if the real-time concentration beta is within the third preset concentration range beta 03, enabling the first polymer to meet preset conditions, adding the aqueous solution into the reactor through the third discharge port, uniformly mixing by using the second stirrer, and in the process, obtaining a value of a real-time average density rho of the intermediate polymer, and if the real-time average density rho of the intermediate polymer is within a first preset average density range rho 11, controlling the second stirring regulator to enable the stirring paddle to be a large stirring paddle Bb2 of the second stirrer, wherein the stirring speed is a second stirring speed Vb2 of the second stirrer, if the real-time average density rho of the intermediate polymer is within a second preset average density range rho 12, controlling the second stirring regulator to enable the stirring paddle to be a small stirring paddle Bb1 of the second stirrer, wherein the stirring speed is a first stirring speed Vb1 of the second stirrer, and if the real-time average density rho of the intermediate polymer is within a third preset average density range rho 13, enabling the intermediate polymer to meet preset conditions.

Further, measuring the temperature in the reactor in real time by using a first temperature measuring instrument;

the central control module is also provided with a reactor preset temperature matrix Ha (Ha 1, Ha2, Ha3), wherein Ha1 represents a first preset reaction temperature, Ha2 represents a second preset reaction temperature, and Ha3 represents a third preset reaction temperature;

the third feed opening is provided with a second control valve for controlling the opening/closing of the third feed opening;

the central control module is also provided with a reaction time matrix T (T1, T2, T3), wherein T1 represents a first reaction time, T2 represents a second reaction time, and T3 represents a third reaction time;

the central control module is also provided with a preset latex viscosity matrix mu 0 (mu 1, mu 2 and mu 3), wherein mu 1 represents a first preset latex viscosity, mu 2 represents a second preset latex viscosity, and mu 3 represents a third preset latex viscosity;

the central control module is also provided with an aqueous solution increment matrix m (m1, m2, m3), wherein m1 represents a first increment of aqueous solution, m2 represents a second increment of aqueous solution, and m3 represents a third increment of aqueous solution;

the acidity measuring instrument is provided with a standard hydrogen ion concentration index of P0;

at a first reaction time T1, if the viscosity of the latex is less than the viscosity of the first preset latex, the first temperature regulator is regulated to a first preset reaction temperature Ha1 through the central control module;

if the viscosity mu of the latex is more than or equal to a second preset latex viscosity mu 2, adjusting the second control valve through the central control module, and adding a first increment m1 of the aqueous solution;

if the first preset latex viscosity mu 1 is not less than the latex viscosity mu and less than the second preset latex viscosity mu 2, obtaining a value of a hydrogen ion concentration index, if the hydrogen ion concentration index P is less than the standard hydrogen ion concentration index P0, adjusting the second control valve through the central control module, adding a first increment m1 of an aqueous solution, if the hydrogen ion concentration index P is greater than the standard hydrogen ion concentration index P0, adjusting the first temperature regulator to a first preset reaction temperature Ha1 through the central control module, and if the hydrogen ion concentration index P is equal to the standard hydrogen ion concentration index P0, enabling the second polymer to meet preset conditions.

Further, at a second reaction time T2, if the viscosity μ of the latex is less than a second predetermined viscosity μ 2 of the latex, adjusting the first temperature regulator to a second predetermined reaction temperature Ha2 by the central control module;

if the viscosity mu of the latex is more than or equal to a third preset latex viscosity mu 3, adjusting the second control valve through the central control module, and adding a second increment m2 of the aqueous solution;

if the second preset latex viscosity mu 2 is not less than the latex viscosity mu and is less than the third preset latex viscosity mu 3, obtaining a value of a hydrogen ion concentration index, if the hydrogen ion concentration index P is less than the standard hydrogen ion concentration index P0, adjusting the second control valve through the central control module, adding a second increment m2 of the aqueous solution, if the hydrogen ion concentration index P is greater than the standard hydrogen ion concentration index P0, adjusting the first temperature regulator to a second preset reaction temperature Ha2 through the central control module, and if the hydrogen ion concentration index P is equal to the standard hydrogen ion concentration index P0, enabling the second polymer to meet preset conditions.

Further, at a third reaction time T3, if the viscosity μ of the latex is less than a third preset viscosity μ 3 of the latex, adjusting the first temperature regulator to a third preset reaction temperature Ha3 by the central control module;

and if the viscosity mu of the latex is more than or equal to a third preset latex viscosity mu 3, adjusting the second control valve through the central control module, and adding a third increment m3 of the aqueous solution.

Further, the central control module is further provided with a preset conversion rate matrix eta 0 (eta 1, eta 2, eta 3), wherein eta 1 represents a first preset conversion rate, eta 2 represents a second preset conversion rate, and eta 3 represents a third preset conversion rate;

the central control module is also provided with a preset polymerization reaction rate matrix R0(R1, R2, R3), wherein R1 represents a first preset polymerization reaction rate, R2 represents a second preset polymerization reaction rate, and R3 represents a third preset polymerization reaction rate;

the central control module is also provided with a reaction temperature increment matrix delta Ha (delta Ha1, delta Ha2, delta Ha3), wherein the delta Ha1 represents a first reaction temperature increment, the delta Ha2 represents a second reaction temperature increment, and the delta Ha3 represents a third reaction temperature increment;

in the second step, at a certain determined moment, if the conversion rate η is less than a first preset conversion rate η 1, the central control module adjusts the first temperature regulator to a first preset reaction temperature Ha1 to obtain a value of a polymerization reaction rate R, if the polymerization reaction rate R is less than a first preset polymerization reaction rate R1, the central control module adjusts the first temperature regulator to increase a first reaction temperature increment Δ Ha1, and if the polymerization reaction rate R is greater than or equal to a first preset polymerization reaction rate R1, the polymerization reaction is sufficient;

if the conversion rate eta is larger than or equal to a first preset conversion rate eta 1, obtaining the value of the polymerization reaction rate R, if the polymerization reaction rate R is smaller than the first preset polymerization reaction rate R1, adjusting the first temperature regulator through the central control module, increasing the first reaction temperature increment delta Ha1, and if the polymerization reaction rate R is larger than or equal to the first preset polymerization reaction rate R1, fully polymerizing.

Further, in the second step, at a certain determined moment, if the conversion rate η is less than a second preset conversion rate η 2, the central control module adjusts the first temperature regulator to a second preset reaction temperature Ha2 to obtain a value of a polymerization reaction rate R, if the polymerization reaction rate R is less than a second preset polymerization reaction rate R2, the central control module adjusts the first temperature regulator to increase a second reaction temperature increment Δ Ha2, and if the polymerization reaction rate R is greater than or equal to a second preset polymerization reaction rate R2, the polymerization reaction is sufficient;

if the conversion rate eta is larger than or equal to a second preset conversion rate eta 2, obtaining the value of the polymerization reaction rate R, if the polymerization reaction rate R is smaller than the second preset polymerization reaction rate R2, adjusting the first temperature regulator through the central control module, increasing the second reaction temperature increment delta Ha2, and if the polymerization reaction rate R is larger than or equal to the second preset polymerization reaction rate R2, fully performing the polymerization reaction.

Further, in the second step, at a certain determined moment, if the conversion rate η is less than a third preset conversion rate η 3, the central control module adjusts the first temperature regulator to a third preset reaction temperature Ha3 to obtain a value of a polymerization reaction rate R, if the polymerization reaction rate R is less than a third preset polymerization reaction rate R3, the central control module adjusts the first temperature regulator to increase a third reaction temperature increment Δ Ha3, and if the polymerization reaction rate R is greater than or equal to the third preset polymerization reaction rate R3, the polymerization reaction is sufficient;

if the conversion rate eta is larger than or equal to a third preset conversion rate eta 3, obtaining the value of the polymerization reaction rate R, if the polymerization reaction rate R is smaller than the third preset polymerization reaction rate R3, adjusting the first temperature regulator through the central control module, increasing the third reaction temperature increment delta Ha3, and if the polymerization reaction rate R is larger than or equal to the third preset polymerization reaction rate R3, fully performing the polymerization reaction.

Further, the temperature in the degassing container is measured in real time by a second temperature measuring instrument;

the central control module is further provided with a preset degassing container temperature matrix Hb (Hb1, Hb2, Hb3), wherein Hb1 represents a first preset degassing temperature, Hb2 represents a second preset degassing temperature, and Hb3 represents a third preset degassing temperature;

the central control module is further provided with a preset water content matrix Q0 (Q1, Q2, Q3), wherein Q1 represents a first preset water content, Q2 represents a second preset water content, and Q3 represents a third preset water content;

the degassing container is provided with a second temperature regulator for regulating the temperature in the degassing container;

the central control module is also provided with a modifier increment matrix M (M1, M2, M3), wherein M1 represents a first increment of modifier, M2 represents a second increment of modifier, and M3 represents a third increment of modifier;

the second feed opening is provided with a first control valve for controlling the opening/closing of the second feed opening;

in the third step, if the water content Q measured by the water content measuring instrument = a first preset water content Q1, adjusting the first control valve through the central control module, adding a first increment M1 of a modifier, and adjusting the second temperature regulator to a first preset degassing temperature Hb1 through the central control module;

if the water content Q = a second preset water content Q2 measured by the water content measuring instrument, adjusting the first control valve through the central control module, adding a second increment M2 of modifier, and adjusting the second temperature regulator to a second preset degassing temperature Hb2 through the central control module;

if the water content Q = a third preset water content Q3, the first control valve is adjusted by the central control module, a third increment M3 of modifier is added, and the second temperature regulator is adjusted by the central control module to a third preset degassing temperature Hb 3.

Further, the central control module comprises a receiving module, a display module and a control module, the display module is respectively connected with the receiving module and the control module, the receiving module is used for receiving the reaction data of the reactor and the degassing container, the display module is provided with a display for displaying the reaction data received by the receiving module, and the control module is used for adjusting the reaction process according to the reaction data.

Further, the aqueous solution is a mixture of an initiator, an emulsifier, a molecular weight regulator and water.

Compared with the prior art, the method has the advantages that the carboxylic styrene-butadiene latex is added into the reactor through the first discharge port, the modifier is added into the reactor through the second discharge port, the mixture is uniformly mixed through the first stirrer to form the first polymer, in the process, the bubble density of the first polymer is detected in real time through the bubble density detector, the concentration of the first polymer is detected in real time through the concentration detector, the preset bubble density matrix a 0 (alpha 01, alpha 02, alpha 03, …, alpha 0 n) and the preset concentration range matrix beta 0 (beta 01, beta 02, beta 03) are set, the real-time measured value of the bubble density is compared with the preset value, the real-time measured value of the concentration is compared with the preset value, the first polymer meets the preset condition through controlling the stirring speed of the first stirrer and the size of the stirring paddle, and then the aqueous solution is added into the reactor through the third discharge port, uniformly mixing the mixture by using a second stirrer to form an intermediate polymer, in the process, obtaining a density matrix rho 0 (rho 1i, rho 2i and rho 3 i) of the intermediate polymer by using a density detector, obtaining the real-time average density of the intermediate polymer by calculation, comparing the real-time measured and calculated value of the average density with a preset value, enabling the intermediate polymer to meet the preset condition by controlling the stirring speed of the second stirrer and the size of a stirring paddle, then adjusting a first temperature regulator by using a central control module to enable the aqueous solution and the first polymer to have polymerization reaction to form a second polymer, then performing water vapor evaporation on the second polymer by using a degassing container to form a third polymer, finally packaging and discharging the third polymer by using a batch mixing container to obtain the packaged modified carboxylic styrene-butadiene latex, so that the first polymer can be prepared by adjusting the stirring speed of the first stirrer and the stirring speed of the second stirrer and the size of the stirring paddle The compound and the intermediate polymer accord with preset conditions, the size of the corresponding stirring paddle is selected by detecting the bubble density in the first polymer, and the rotating speed of the stirring paddle is adjusted in a targeted manner, so that the mixing degree of the first polymer reaches a preset standard, the reaction speed of the first polymer is effectively increased, and the preparation efficiency of the process for the modified carboxylic styrene-butadiene latex is improved.

Further, the latex viscosity of the second polymer is measured in real time by using a viscosity measuring instrument, the hydrogen ion concentration index of the second polymer is measured in real time by using an acidity measuring instrument, a reaction time matrix T (T1, T2, T3) and an aqueous solution increment matrix m (m1, m2, m3) are set, the measured value of the latex viscosity is compared with a preset value at a certain reaction moment, the latex viscosity meets the preset value by adjusting the temperature and the hydrogen ion concentration index, so that the second polymer meets the preset condition, the polymerization reaction in a reactor can be controlled by adjusting the temperature and the hydrogen ion concentration index, the second polymer meets the preset condition, the preparation process is simple, the reaction efficiency is improved, the labor cost of a complex process is saved, and the safety is improved by remotely controlling the reaction process by using a central control module.

Drawings

FIG. 1 is a schematic structural view of a modified carboxylated styrene-butadiene latex manufacturing apparatus according to the present invention;

FIG. 2 is a schematic flow diagram of a process for preparing a modified carboxylated styrene-butadiene latex according to the present invention;

in the figure: 1-a reactor; 11-a first feed opening; 12-a second feed opening; 121-a first control valve; 13-a first stirrer; 131-a second stirrer; 14-a third feed opening; 141-a second control valve; 15-a first temperature regulator; 16-conversion measuring instrument; 17-polymerization rate measuring instrument; 18-viscosity measuring instrument; 19-acidity meter; 101-a first temperature measuring instrument; 2-a degassing vessel; 21-water content measuring instrument; 22-a second temperature regulator; 23-a second temperature measuring instrument; 3-mixing batch container; 4-a central control module; 41-a receiving module; 42-a display module; 43-control module.

Detailed Description

In order that the objects and advantages of the invention will be more clearly understood, the invention is further described below with reference to examples; it should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention.

Preferred embodiments of the present invention are described below with reference to the accompanying drawings. It should be understood by those skilled in the art that these embodiments are only for explaining the technical principle of the present invention, and do not limit the scope of the present invention.

It should be noted that in the description of the present invention, the terms of direction or positional relationship indicated by the terms "upper", "lower", "left", "right", "inner", "outer", etc. are based on the directions or positional relationships shown in the drawings, which are only for convenience of description, and do not indicate or imply that the device or element must have a specific orientation, be constructed in a specific orientation, and be operated, and thus, should not be construed as limiting the present invention.

Furthermore, it should be noted that, in the description of the present invention, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood by those skilled in the art according to specific situations.

Referring to fig. 1 and 2, fig. 1 is a schematic structural diagram of a modified carboxylated styrene-butadiene latex preparation device according to the present invention, and fig. 2 is a schematic flow diagram of a modified carboxylated styrene-butadiene latex preparation process according to the present invention. The preparation device of the modified carboxylic styrene-butadiene latex of the embodiment of the invention comprises: the system comprises a reactor 1, a first feed opening 11, a second feed opening 12, a first control valve 121, a first stirrer 13, a second stirrer 131, a third feed opening 14, a second control valve 141, a first temperature regulator 15, a conversion rate measuring instrument 16, a polymerization reaction rate measuring instrument 17, a viscosity measuring instrument 18, an acidity measuring instrument 19, a first temperature measuring instrument 101, a degassing container 2, a water content measuring instrument 21, a second temperature measuring instrument 23, a second temperature regulator 22, a mixing container 3, a central control module 4, a receiving module 41, a display module 42 and a control module 43.

The reactor 1 is used for loading a first polymer and a second polymer; the first feed opening 11, the second feed opening 12 and the third feed opening 14 are all arranged on the reactor 1, the first feed opening 11 is used for adding carboxylic styrene-butadiene latex, the second feed opening 12 is used for adding a modifier, and the third feed opening 14 is used for adding an aqueous solution; the first control valve 121 is disposed on the second feed opening 12, and is used for controlling the opening/closing of the second feed opening 12; the second control valve 141 is disposed on the third feed opening 14, and is used for controlling the third feed opening 14 to open/close; the first stirrer 13 and the second stirrer 131 are both arranged in the reactor 1, the first stirrer 13 is used for uniformly mixing the carboxylated styrene-butadiene latex and the modifier, and the second stirrer 131 is used for uniformly mixing the first polymer and the aqueous solution; the first temperature regulator 15 is provided on the reactor 1 to regulate the temperature of the intermediate polymer; the conversion rate measuring instrument 16, the polymerization reaction rate measuring instrument 17, the viscosity measuring instrument 18, the acidity measuring instrument 19 and the first temperature measuring instrument 101 are all arranged in the reactor 1, the conversion rate measuring instrument 16 is used for measuring the conversion rate of the polymerization reaction in real time, the polymerization reaction rate measuring instrument 17 is used for measuring the rate of the polymerization reaction in real time, the viscosity measuring instrument 18 is used for measuring the latex viscosity of the second polymer in real time, the acidity measuring instrument 19 is used for measuring the hydrogen ion concentration index of the second polymer in real time, and the first temperature measuring instrument 101 is used for measuring the temperature in the reactor 1 in real time.

The degassing container 2 is connected with the reactor 1 and is used for carrying out vapor evaporation on the second polymer to form a third polymer; the water content meter 21, the second temperature regulator 22 and the second temperature meter 23 are all disposed within the degassing vessel 2, the water content meter 21 is used to measure the water content of the third polymer in real time, the second temperature regulator 22 is used to regulate the temperature of the degassing vessel 2, and the second temperature meter 23 is used to measure the temperature in the degassing vessel 2 in real time.

The mixing container 3 is connected with the degassing container 2 and is used for packing and discharging the third polymer.

The central control module 4 is connected with the mixed batch container 3 and used for controlling the reaction process, and a matrix is arranged in the central control module; the central control module 4 comprises the receiving module 41, the display module 42 and the control module 43, the display module 42 is respectively connected with the receiving module 41 and the control module 43, the receiving module 41 is used for receiving the reaction data of the reactor 1 and the degassing container 2, the display module 42 is provided with a display for displaying the reaction data received by the receiving module 41, and the control module 43 is used for adjusting the reaction process according to the reaction data. The receiving module 41 in the embodiment of the present invention receives the reaction data in the degassing container 2 in the reactor 1 and then transmits the reaction data to the display module 42 for display, and the control module 43 adjusts the reaction process according to the reaction data displayed on the display module 42, so that the reaction process can be remotely controlled, and the safety is improved.

Referring to fig. 1, based on the above apparatus for preparing modified carboxylated styrene-butadiene latex, the process of preparing modified carboxylated styrene-butadiene latex of this embodiment includes: step one, adding carboxylic styrene-butadiene latex into a reactor 1 through a first feed opening 11, adding a modifier into the reactor 1 through a second feed opening 12, uniformly mixing by using a first stirrer 13 to form a first polymer, detecting the bubble density of the first polymer in real time by using a bubble density detector, wherein the detected real-time bubble density is alpha, and detecting the concentration of the first polymer in real time by using a concentration detector, wherein the detected real-time concentration is beta; step two, adding an aqueous solution into the reactor 1 through a third feed opening 14, uniformly mixing by using a second stirrer 131 to form an intermediate polymer, adjusting a first temperature regulator 15 to enable the aqueous solution and the first polymer to generate a polymerization reaction to form a second polymer, measuring the conversion rate of the polymerization reaction in real time by using a conversion rate measuring instrument 16, wherein the measured conversion rate is eta, measuring the polymerization reaction rate in real time by using a polymerization reaction rate measuring instrument 17, the measured polymerization reaction rate is R, measuring the latex viscosity of the second polymer in real time by using a viscosity measuring instrument 18, the measured latex viscosity is mu, measuring the hydrogen ion concentration index of the second polymer in real time by using an acidity measuring instrument 19, and the measured hydrogen ion concentration index is P; thirdly, evaporating water vapor of the second polymer through the degassing container 2 to form a third polymer, and measuring the water content of the third polymer in real time by using a water content measuring instrument 21, wherein the measured water content is Q; step four, packing and discharging the third polymer through a batch mixing container 3; wherein, the reactor 1 and the degassing container 2 are connected with a central control module 4 through wireless, the central control module 4 is used for controlling the reaction process from the first step to the third step, and a matrix is arranged in the central control module 4; the first stirrer 13 is provided with a first stirring regulator for regulating the stirring speed of the first stirrer 13 and the size of a stirring paddle of the first stirrer 13; the central control module 4 is provided with a preset bubble density matrix α 0(α 01, α 02, α 03, …, α 0 n), α 01 < α 02 < α 03 < … < α 0n, wherein α 01 represents a first preset bubble density, α 02 represents a second preset bubble density, and α 03 represents a third preset bubble density, …, and α 0n nth preset bubble density; the central control module 4 is further provided with a stirring speed matrix Va (Va 1, Va2, Va 3), wherein Va1 represents a first stirring speed of the first stirrer 13, Va2 represents a second stirring speed of the first stirrer 13, and Va3 represents a third stirring speed of the first stirrer 13; the central module 4 is further provided with a paddle matrix Ba (Ba 1, Ba 2), the Ba1 representing a small paddle of the first stirrer 13, the Ba2 representing a large paddle of the first stirrer 13; the central control module 4 is further provided with a preset concentration range matrix beta 0 (beta 01, beta 02, beta 03), wherein beta 01 is greater than beta 02 and is greater than beta 03, wherein beta 01 represents a first preset concentration range, beta 02 is a second preset concentration range, and beta 03 represents a third preset concentration range; the second stirrer 131 is provided with a second stirring regulator for regulating the stirring speed of the second stirrer 131 and the size of the stirring paddle of the second stirrer 131; the central module 4 is also provided with a stirring speed matrix Vb (Vb 1, Vb 2), wherein Vb1 represents the first stirring speed of the second stirrer 131, and Vb2 represents the second stirring speed of the second stirrer 131; the central control module 4 is further provided with a stirring paddle matrix Bb (Bb 1, Bb 2), where Bb1 represents the small stirring paddle of the second stirrer 131, and Bb2 represents the large stirring paddle of the second stirrer 131; the second stirrer 131 has a preset length L and is provided with a density detector, the density detector is capable of detecting real-time densities of different positions of the second stirrer 131 in the vertical direction, wherein the uppermost first density detection point is set to obtain a first density matrix ρ 1i at different times, the middle second density detection point is set to obtain a second density matrix ρ 2i at different times, the lowermost third density detection point is set to obtain a third density matrix ρ 3i at different times, and a density matrix ρ 0(ρ 1i, ρ 2i, ρ 3 i) of the intermediate polymer is formed to calculate the real-time average density ρ of the intermediate polymer, and the calculation formula is as follows:

where ρ 1i represents a first density matrix, ρ 2i represents a second density matrix, and ρ 3i represents a third density matrix; the density detector is internally provided with a control unit which is a PLC control panel, and an intermediate polymer preset average density matrix rho a (rho 11, rho 12, rho 13) is arranged in the PLC control panel, wherein rho 11 represents a first intermediate polymer preset average density range, rho 12 represents a second intermediate polymer preset average density range, and rho 13 represents a third intermediate polymer preset average density range; if the real-time bubble density α is less than the first preset bubble density α 01, controlling the first stirring regulator to make the stirring speed be the first stirring speed Va1 of the first stirrer 13; if the real-time bubble density α > nth preset bubble density α 0n, controlling the first stirring regulator to enable the stirring speed to be the third stirring speed Va3 of the first stirrer 13; if the first preset bubble density alpha 01 is not greater than the real-time bubble density alpha 0n, controlling the first stirring regulator to enable the stirring speed to be the second stirring speed Va2 of the first stirrer 13 to obtain a value of the real-time concentration beta, if the real-time concentration beta is within the first preset concentration range beta 01, controlling the first stirring regulator to enable the stirring paddle to be a large stirring paddle Ba2 of the first stirrer 13, if the real-time concentration beta is within the second preset concentration range beta 02, controlling the first stirring regulator to enable the stirring paddle to be a small stirring paddle Ba1 of the first stirrer 13, and if the real-time concentration beta is within the third preset concentration range beta 03, controlling the first stirring regulator to enable the stirring paddle to be a small stirring paddle Ba1 of the first stirrer 13When a polymer meets a preset condition, adding the aqueous solution into the reactor 1 through the third feed opening 14, uniformly mixing by using the second stirrer 131, in the process, obtaining a value of the real-time average density ρ of the intermediate polymer, controlling the second stirring regulator to make the stirring paddle be a large stirring paddle Bb2 of the second stirrer 131 and the stirring speed be a second stirring speed Vb2 of the second stirrer 131 if the real-time average density ρ of the intermediate polymer is within a first preset average density range ρ 11, controlling the second stirring regulator to make the stirring paddle be a small stirring paddle Bb1 of the second stirrer 131 and the stirring speed be a first stirring speed Vb1 of the second stirrer 131 if the real-time average density ρ of the intermediate polymer is within a second preset average density range ρ 12, and if the real-time average density ρ of the intermediate polymer is within a third preset average density range ρ 13, the intermediate polymer meets the preset conditions. In the embodiment of the present invention, the first feed opening 11 adds the carboxylated styrene-butadiene latex into the reactor 1, the second feed opening 12 adds the modifier into the reactor 1, the mixture is uniformly mixed by the first mixer 13 to form the first polymer, in this process, the bubble density of the first polymer is detected in real time by using the bubble density detector, the concentration of the first polymer is detected in real time by using the concentration detector, a preset bubble density matrix a 0 (a 01, a 02, a 03, …, a 0 n) and a preset concentration range matrix β 0(β 01, β 02, β 03) are set, the real-time measurement value of the bubble density is compared with a preset value, the real-time measurement value of the concentration is compared with the preset value, the first polymer meets the preset condition by controlling the mixing speed of the first mixer 13 and the size of the mixing paddle, and then the aqueous solution is added into the reactor 1 by the third feed opening 14, uniformly mixing the mixture by using the second stirrer 131 to form an intermediate polymer, in the process, obtaining a density matrix rho 0 (rho 1i, rho 2i, rho 3 i) of the intermediate polymer by using a density detector, obtaining the real-time average density of the intermediate polymer by calculation, comparing the real-time measured and calculated value of the average density with a preset value, enabling the intermediate polymer to accord with the preset condition by controlling the stirring speed of the second stirrer 131 and the size of a stirring paddle, and then adjusting the first temperature by using a central control module 4The regulator 15 makes the aqueous solution and the first polymer generate polymerization reaction to form a second polymer, then the second polymer is subjected to water vapor evaporation through the degassing container 2 to form a third polymer, and finally the third polymer is packed and discharged through the mixing container 3 to obtain the packaged modified carboxylic styrene-butadiene latex, so that the first polymer and the intermediate polymer can meet the preset conditions by adjusting the stirring speed of the first stirrer 13 and the second stirrer 131 and the size of the stirring paddle, the preparation process is simple, the reaction efficiency is further improved, and the labor cost of a complex process is saved.

Specifically, the temperature in the reactor 1 is measured in real time by the first temperature measuring instrument 101; the central control module 4 is further provided with a reactor 1 preset temperature matrix Ha (Ha 1, Ha2, Ha3), wherein Ha1 represents a first preset reaction temperature, Ha2 represents a second preset reaction temperature, and Ha3 represents a third preset reaction temperature; the third feed opening 14 is provided with a second control valve 141 for controlling the opening/closing of the third feed opening 14; the central control module 4 is further provided with a reaction time matrix T (T1, T2, T3), wherein T1 represents a first reaction time, T2 represents a second reaction time, and T3 represents a third reaction time; the central control module 4 is further provided with a preset latex viscosity matrix mu 0 (mu 1, mu 2 and mu 3), wherein mu 1 represents a first preset latex viscosity, mu 2 represents a second preset latex viscosity, and mu 3 represents a third preset latex viscosity; the central control module 4 is also provided with an aqueous solution increment matrix m (m1, m2, m3), wherein m1 represents a first increment of aqueous solution, m2 represents a second increment of aqueous solution, and m3 represents a third increment of aqueous solution; the acidity measuring instrument 19 is provided with a standard hydrogen ion concentration index of P0, and at a first reaction time T1, if the viscosity mu of the latex is less than a first preset latex viscosity mu 1, the central control module 4 adjusts the first temperature regulator 15 to a first preset reaction temperature Ha 1; if the viscosity mu of the latex is more than or equal to a second preset latex viscosity mu 2, adjusting the second control valve 141 through the central control module 4, and adding a first increment m1 of the aqueous solution; if the first preset latex viscosity mu 1 is not less than the latex viscosity mu and is less than the second preset latex viscosity mu 2, obtaining a value of a hydrogen ion concentration index, if the hydrogen ion concentration index P is less than the standard hydrogen ion concentration index P0, adjusting the second control valve 141 through the central control module 4, adding a first increment m1 of an aqueous solution, if the hydrogen ion concentration index P is greater than the standard hydrogen ion concentration index P0, adjusting the first temperature regulator 15 to a first preset reaction temperature Ha1 through the central control module 4, and if the hydrogen ion concentration index P is equal to the standard hydrogen ion concentration index P0, enabling the second polymer to meet preset conditions. In the embodiment of the present invention, the viscosity of the latex of the second polymer is measured in real time by the viscosity measuring instrument 18, the hydrogen ion concentration index of the second polymer is measured in real time by the acidity measuring instrument 19, the reaction time matrix T (T1, T2, T3) and the aqueous solution increment matrix m (m1, m2, m3) are set, and at a certain reaction time, comparing the measured value of the latex viscosity with a preset value, enabling the latex viscosity to accord with the preset value by adjusting the temperature and the hydrogen ion concentration index, thereby enabling the second polymer to accord with the preset conditions, controlling the polymerization reaction in the reactor 1 by adjusting the temperature and the hydrogen ion concentration index, enabling the second polymer to accord with the preset conditions, having simple preparation process, and further, the reaction efficiency is improved, the labor cost of a complex process is saved, and the safety is improved by remotely controlling the reaction process through the central control module 4.

Specifically, at a second reaction time T2, if the viscosity μ of the latex is less than a second predetermined viscosity μ 2 of the latex, the first temperature regulator 15 is regulated to a second predetermined reaction temperature Ha2 by the central control module 4; if the viscosity mu of the latex is more than or equal to a third preset latex viscosity mu 3, adjusting the second control valve 141 through the central control module 4, and adding a second increment m2 of the aqueous solution; if the second preset latex viscosity mu 2 is not less than the latex viscosity mu and is less than the third preset latex viscosity mu 3, obtaining a value of a hydrogen ion concentration index, if the hydrogen ion concentration index P is less than the standard hydrogen ion concentration index P0, adjusting the second control valve 141 through the central control module 4, adding a second increment m2 of the aqueous solution, if the hydrogen ion concentration index P is greater than the standard hydrogen ion concentration index P0, adjusting the first temperature regulator 15 to a second preset reaction temperature Ha2 through the central control module 4, and if the hydrogen ion concentration index P is equal to the standard hydrogen ion concentration index P0, enabling the second polymer to meet preset conditions. Therefore, the polymerization reaction in the reactor 1 can be controlled by adjusting the temperature and the hydrogen ion concentration index, the preparation process is simple, the reaction efficiency is improved, the labor cost of a complex process is saved, and the safety is improved by remotely controlling the reaction process through the central control module 4.

Specifically, at a third reaction time T3, if the viscosity μ of the latex is less than a third preset viscosity μ 3 of the latex, the first temperature regulator 15 is regulated to a third preset reaction temperature Ha3 by the central control module 4; if the viscosity mu of the latex is more than or equal to a third preset latex viscosity mu 3, the second control valve 141 is adjusted through the central control module 4, and a third increment m3 of the aqueous solution is added. The viscosity measuring instrument 18 in the embodiment of the present invention measures the latex viscosity of the second polymer in real time, the acidity measuring instrument 19 measures the hydrogen ion concentration index of the second polymer in real time, at the third reaction time T3, the measured value of the latex viscosity is compared with the preset value, if the measured value is smaller than the preset value, the temperature of the first temperature regulator 15 is adjusted by the central control module 4, so that the latex viscosity is increased, and if the measured value is greater than or equal to the preset value, the second control valve 141 is adjusted by the central control module 4, and a certain amount of aqueous solution is added, so that the latex viscosity is decreased. Therefore, the polymerization reaction in the reactor 1 can be controlled by adjusting the temperature and the hydrogen ion concentration index, the preparation process is simple, the reaction efficiency is improved, the labor cost of a complex process is saved, and the safety is improved by remotely controlling the reaction process through the central control module 4.

Specifically, the central control module 4 is further provided with a preset conversion rate matrix η 0(η 1, η 2, η 3), where η 1 represents a first preset conversion rate, η 2 represents a second preset conversion rate, and η 3 represents a third preset conversion rate; the central control module 4 is further provided with a preset polymerization rate matrix R0(R1, R2, R3), wherein R1 represents a first preset polymerization rate, R2 represents a second preset polymerization rate, and R3 represents a third preset polymerization rate; the central control module 4 is further provided with a reaction temperature increment matrix Δ Ha (Δ Ha1, Δ Ha2, Δ Ha3), wherein Δ Ha1 represents a first reaction temperature increment, Δ Ha2 represents a second reaction temperature increment, and Δ Ha3 represents a third reaction temperature increment; in the second step, at a certain determined moment, if the conversion rate η is less than a first preset conversion rate η 1, the central control module 4 adjusts the first temperature regulator 15 to a first preset reaction temperature Ha1 to obtain a value of a polymerization reaction rate R, if the polymerization reaction rate R is less than a first preset polymerization reaction rate R1, the central control module 4 adjusts the first temperature regulator 15 to increase a first reaction temperature increment Δ Ha1, and if the polymerization reaction rate R is greater than or equal to the first preset polymerization reaction rate R1, the polymerization reaction is sufficient; if the conversion rate eta is larger than or equal to a first preset conversion rate eta 1, obtaining the value of the polymerization reaction rate R, if the polymerization reaction rate R is smaller than the first preset polymerization reaction rate R1, adjusting the first temperature regulator 15 through the central control module 4, increasing the first reaction temperature increment delta Ha1, and if the polymerization reaction rate R is larger than or equal to the first preset polymerization reaction rate R1, fully performing the polymerization reaction. Therefore, the conversion rate of the polymerization reaction can be controlled by adjusting the temperature and the polymerization reaction rate, the polymerization reaction rate is controlled by adjusting the temperature, the polymerization reaction can be more sufficient, the conversion rate of the polymerization reaction is improved, the raw material cost is saved, and the safety is improved by remotely controlling the reaction process through the central control module 4.

Specifically, in the second step, at a certain determined moment, if the conversion rate η is less than a second preset conversion rate η 2, the central control module 4 adjusts the first temperature regulator 15 to a second preset reaction temperature Ha2 to obtain a value of a polymerization reaction rate R, if the polymerization reaction rate R is less than a second preset polymerization reaction rate R2, the central control module 4 adjusts the first temperature regulator 15 to increase a second reaction temperature increment Δ Ha2, and if the polymerization reaction rate R is greater than or equal to the second preset polymerization reaction rate R2, the polymerization reaction is sufficient; if the conversion rate eta is larger than or equal to a second preset conversion rate eta 2, obtaining the value of the polymerization reaction rate R, if the polymerization reaction rate R is smaller than the second preset polymerization reaction rate R2, adjusting the first temperature regulator 15 through the central control module 4, increasing the second reaction temperature increment delta Ha2, and if the polymerization reaction rate R is larger than or equal to the second preset polymerization reaction rate R2, fully performing the polymerization reaction. Therefore, the conversion rate of the polymerization reaction can be controlled by adjusting the temperature and the polymerization reaction rate, the polymerization reaction rate is controlled by adjusting the temperature, the polymerization reaction can be more sufficient, the conversion rate of the polymerization reaction is improved, the raw material cost is saved, and the safety is improved by remotely controlling the reaction process through the central control module 4.

Specifically, in the second step, at a certain determined moment, if the conversion rate η is less than a third preset conversion rate η 3, the central control module 4 adjusts the first temperature regulator 15 to a third preset reaction temperature Ha3 to obtain a value of a polymerization reaction rate R, if the polymerization reaction rate R is less than a third preset polymerization reaction rate R3, the central control module 4 adjusts the first temperature regulator 15 to increase a third reaction temperature increment Δ Ha3, and if the polymerization reaction rate R is greater than or equal to the third preset polymerization reaction rate R3, the polymerization reaction is sufficient; if the conversion rate eta is larger than or equal to a third preset conversion rate eta 3, obtaining the value of the polymerization reaction rate R, if the polymerization reaction rate R is smaller than the third preset polymerization reaction rate R3, adjusting the first temperature regulator 15 through the central control module 4, increasing a third reaction temperature increment delta Ha3, and if the polymerization reaction rate R is larger than or equal to the third preset polymerization reaction rate R3, fully performing the polymerization reaction. Therefore, the conversion rate of the polymerization reaction can be controlled by adjusting the temperature and the polymerization reaction rate, the polymerization reaction rate is controlled by adjusting the temperature, the polymerization reaction can be more sufficient, the conversion rate of the polymerization reaction is improved, the raw material cost is saved, and the safety is improved by remotely controlling the reaction process through the central control module 4.

Specifically, the temperature in the degassing vessel 2 is measured in real time by the second temperature measuring instrument 23; the central control module 4 is also provided with a preset degassing vessel 2 temperature matrix Hb (Hb1, Hb2, Hb3), wherein Hb1 represents a first preset degassing temperature, Hb2 represents a second preset degassing temperature, Hb3 represents a third preset degassing temperature; the central control module 4 is further provided with a preset water cut matrix Q0 (Q1, Q2, Q3), wherein Q1 represents a first preset water cut, Q2 represents a second preset water cut, and Q3 represents a third preset water cut; the degassing vessel 2 is provided with a second temperature regulator 22 for regulating the temperature inside the degassing vessel 2; the central control module 4 is also provided with a modifier increment matrix M (M1, M2, M3), wherein M1 represents a first increment of modifier, M2 represents a second increment of modifier, and M3 represents a third increment of modifier; the second feed opening 12 is provided with a first control valve 121 for controlling the opening/closing of the second feed opening 12; in the third step, if the water content Q measured by the water content measuring instrument 21 = the first preset water content Q1, the first control valve 121 is adjusted by the central control module 4, the first increment M1 of the modifier is added, and the second temperature regulator 22 is adjusted by the central control module 4 to the first preset degassing temperature Hb 1; if the water cut Q = a second preset water cut Q2 measured by the water cut meter 21, adjusting the first control valve 121 by means of the central control module 4, adding a second increment M2 of modifying agent, adjusting the second temperature regulator 22 by means of the central control module 4 to a second preset degassing temperature Hb 2; if the water cut Q = a third predetermined water cut Q3 measured by the water cut meter 21, the first control valve 121 is adjusted by the central control module 4, a third increment M3 of modifying agent is added, and the second temperature regulator 22 is adjusted by the central control module 4 to a third predetermined degassing temperature Hb 3. In the embodiment of the invention, the second temperature measuring instrument 23 measures the temperature in the degassing container 2, the water content measuring instrument 21 is provided with a preset water content matrix Q (Q1, Q2, Q3), the second feed opening 12 is provided with a modifier increment matrix M (M1, M2, M3), in the third step, the measured value of the water content is compared with the preset value, the modifier is added by adjusting the first control valve 121 through the central control module 4, the second temperature regulator 22 is adjusted through the central control module 4, the water content meets the degassing standard, the water content of the third polymer in the degassing container 2 can be controlled by adding the modifier and adjusting the temperature, and the reaction process is remotely controlled through the central control module 4, so that the safety is improved.

Specifically, the aqueous solution is a mixture of an initiator, an emulsifier, a molecular weight regulator and water. The respective contents of the respective substances in the aqueous solution vary depending on the modifier.

So far, the technical solutions of the present invention have been described in connection with the preferred embodiments shown in the drawings, but it is easily understood by those skilled in the art that the scope of the present invention is obviously not limited to these specific embodiments. Equivalent changes or substitutions of related technical features can be made by those skilled in the art without departing from the principle of the invention, and the technical scheme after the changes or substitutions can fall into the protection scope of the invention.

The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention; various modifications and alterations to this invention will become apparent to those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.

Claims

1. A preparation process of modified carboxylic styrene-butadiene latex is characterized by comprising the following steps:

2. The process for preparing a modified carboxylated styrene-butadiene latex according to claim 1, wherein the temperature in the reactor is measured in real time by a first temperature measuring instrument;

3. The process for preparing a modified carboxylated styrene-butadiene latex according to claim 2, wherein at the second reaction time T2, if the viscosity μ of the latex is less than the second predetermined viscosity μ 2, the first temperature regulator is adjusted by the central control module to the second predetermined reaction temperature Ha 2;

4. The process for preparing a modified carboxylated styrene-butadiene latex according to claim 2, wherein at the third reaction time T3, if the viscosity μ of the latex is less than the third preset viscosity μ 3, the first temperature regulator is adjusted by the central control module to the third preset reaction temperature Ha 3;

5. The process for preparing a modified carboxylated styrene-butadiene latex according to claim 1, wherein said central control module is further provided with a predetermined conversion matrix η 0(η 1, η 2, η 3), where η 1 represents a first predetermined conversion, η 2 represents a second predetermined conversion, and η 3 represents a third predetermined conversion;

6. The process for preparing a modified carboxylated styrene-butadiene latex according to claim 5, wherein in said second step, at a certain determined moment, if the conversion η is less than the second predetermined conversion η 2, the central control module adjusts the first temperature regulator to the second predetermined reaction temperature Ha2 to obtain the value of the polymerization rate R, if the polymerization rate R is less than the second predetermined polymerization rate R2, the central control module adjusts the first temperature regulator to increase the second reaction temperature increment Δ Ha2, and if the polymerization rate R is greater than or equal to the second predetermined polymerization rate R2, the polymerization is complete;

7. The process for preparing a modified carboxylated styrene-butadiene latex according to claim 5, wherein in said second step, at a certain determined moment, if the conversion η is less than the third predetermined conversion η 3, the central control module adjusts the first temperature regulator to the third predetermined reaction temperature Ha3 to obtain the value of the polymerization rate R, if the polymerization rate R is less than the third predetermined polymerization rate R3, the central control module adjusts the first temperature regulator to increase the third reaction temperature increment Δ Ha3, and if the polymerization rate R is greater than or equal to the third predetermined polymerization rate R3, the polymerization is complete;

8. The process for producing a modified carboxylated styrene-butadiene latex according to claim 1, wherein the temperature in the degassing vessel is measured in real time by a second temperature measuring instrument;

9. The process according to claim 1, wherein the central control module comprises a receiving module, a display module and a control module, the display module is connected to the receiving module and the control module respectively, the receiving module is used for receiving the reaction data of the reactor and the degassing container, the display module is provided with a display for displaying the reaction data received by the receiving module, and the control module is used for adjusting the reaction process according to the reaction data.

10. The process for preparing modified carboxylated styrene-butadiene latex according to claim 1, wherein said aqueous solution is a mixture of an initiator, an emulsifier, a molecular weight regulator and water.