CN115197377B - Preparation method of continuous bulk polymerization high-absorptivity resin - Google Patents
Preparation method of continuous bulk polymerization high-absorptivity resin Download PDFInfo
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- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F283/00—Macromolecular compounds obtained by polymerising monomers on to polymers provided for in subclass C08G
- C08F283/06—Macromolecular compounds obtained by polymerising monomers on to polymers provided for in subclass C08G on to polyethers, polyoxymethylenes or polyacetals
- C08F283/065—Macromolecular compounds obtained by polymerising monomers on to polymers provided for in subclass C08G on to polyethers, polyoxymethylenes or polyacetals on to unsaturated polyethers, polyoxymethylenes or polyacetals
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- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
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- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
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- B01J19/0013—Controlling the temperature of the process
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- C08F2/00—Processes of polymerisation
- C08F2/01—Processes of polymerisation characterised by special features of the polymerisation apparatus used
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Abstract
The invention provides a preparation method of a continuous bulk polymerization super absorbent resin, which comprises the following steps: step one: preparing a mixture A from vinyl monomers (salts), cross-linking agents with more than two functional groups, dispersing agents and metal ion chelating agents; step two: the mixture A is pumped into a feeding preheating calandria of a polymerization reactor through a plunger pump, and after coming out of the preheating calandria, the mixture A enters a constant temperature heater for heating, then enters a static mixer for mixing with an initiator, finally enters an inner cavity of the polymerization reactor, the center of the inner cavity is a spiral propeller, and the mixture A mixed with the initiator is subjected to bulk polymerization under the conditions of rapid stirring and heating temperature control; step three: the polymer is cut into particles or segments by a rotary cutter, and then enters a curing device for continuous reaction and cooling to obtain a polymer B. The invention can not only greatly reduce the energy consumption intensity of the industrial increment value, but also simultaneously meet the requirements of the technical index of the high-absorptivity resin.
Description
Technical Field
The invention belongs to the field of preparation of high-absorptivity resin, and relates to a continuous bulk polymerization high-absorptivity resin preparation method.
Background
With the action of double control of total energy consumption and energy consumption intensity of an industrial increase value, which are strictly implemented in 2021 in 9 months of China, the energy consumption double control is an important measure for realizing a carbon peak, and the implementation aims to construct an environment-friendly society, create an environment-friendly development economic environment and meet the requirement of sustainable development of the society with less energy consumption. The energy double control is released, implemented and administered to society by the government of China, and both enterprises and masses are required to follow the relevant regulations, and the development strategy of the state of the advocacy is followed.
The existing preparation method of the high-absorptivity resin mainly comprises an aqueous solution polymerization process and a reverse suspension polymerization process, a large amount of water is introduced into monomers before polymerization in the two processes, and the water is completely dried after polymerization, so that the industrial increase value energy consumption intensity of the high-absorptivity resin is high, the production process is very necessary to innovate, the industrial increase value energy consumption intensity is greatly reduced, and the aims of energy conservation and consumption reduction are fulfilled.
In order to greatly reduce the energy consumption strength of the high-absorption resin industry and meet the technical index requirements of the high-absorption resin, the inventor performs a great deal of experiments and intensive researches, and creatively invents a preparation method of the continuous bulk polymerization high-absorption resin.
In summary, in order to solve the defects in the prior art, the invention designs a continuous bulk polymerization high-absorbent resin preparation method which can not only greatly reduce the energy consumption in the preparation process of the high-absorbent resin, but also simultaneously meet the technical index requirements of the high-absorbent resin.
Disclosure of Invention
The invention provides a continuous bulk polymerization high-absorptivity resin preparation method for solving the problems in the prior art, and the high-absorptivity resin prepared by the preparation system can not only greatly reduce the energy consumption strength of an industrial added value, but also complete the tasks of energy conservation and consumption reduction, and can also simultaneously meet the requirements of the technical indexes of the high-absorptivity resin.
The aim of the invention can be achieved by the following technical scheme:
a method for preparing a continuous mass polymerized superabsorbent resin, comprising:
step one: preparing a mixture A from vinyl monomers (salts), cross-linking agents with more than two functional groups, dispersing agents and metal ion chelating agents;
step two: the mixture A is pumped into a feeding preheating calandria of a polymerization reactor through a plunger pump, and after coming out of the preheating calandria, the mixture A enters a constant temperature heater for heating, then enters a static mixer for mixing with an initiator, finally enters an inner cavity of the polymerization reactor, the center of the inner cavity is a spiral propeller, and the mixture A mixed with the initiator is subjected to bulk polymerization under the conditions of rapid stirring and heating temperature control;
step three: the polymer is extruded from the outlet of the polymerization reactor, then is cut into particles or segments by a rotary cutter, and enters a curing device for continuous reaction and cooling to obtain a polymer B;
step four: the polymer B is crushed or ground, screened and surface treated to obtain the final product C.
As a further improvement of the present embodiment, the vinyl monomer (salt) in the first step is at least one selected from the group consisting of carboxylic acid (salt) group, sulfonic acid (salt) group, phosphoric acid (salt) group and hydroxyl group having a double bond.
As a further improvement of the present embodiment, the above-mentioned two-functional crosslinking agent in the first step is at least one selected from the group consisting of a polyol diglycidyl ether, a polyol (di-tetra) acrylate, a polyol (di-tetra) allyl ether, and a polyol diglycidyl ether;
as a further improvement of the scheme, the temperature rise range of the mixture A from the inlet to the outlet of the preheating calandria in the second step is 8-32 ℃, and the temperature control range of the mixture A at the outlet of the constant temperature heater is 82-125 ℃.
As a further improvement of the scheme, the polymerization reactor in the second step consists of three sections, and the three sections are separated by heat insulation gaskets.
As a further improvement of the scheme, the first section of the inner cavity of the polymerization reactor is an initiating section, the second section is a heat exchange section, and the third section is a strong heat exchange section.
As a further improvement of the scheme, the residence time of the material in the inner cavity of the polymerization reactor is 32-150 seconds.
As a further improvement of the scheme, the screw pitch ratio of the screw of the initiation section and the screw of the heat exchange section of the polymerization reactor is 1:1.2-1:2.2, and the screw pitch ratio of the screw of the initiation section and the screw of the strong heat exchange section of the polymerization reactor is 1:1.2-1:2.2.
As a further improvement of the scheme, the curing device in the third step is in an air-cooled screen plate chain circulation type, the residence time of the materials in the curing device is controlled to be 1-6 minutes, and the temperature control range of the materials at the outlet of the curing device is 70-30 ℃.
As a further improvement of the scheme, the air-cooled screen plate is provided with round holes, the diameter of the round holes is 1.2-5.5 mm, and the aperture ratio of the air-cooled screen plate is 22% -41%.
Compared with the prior art, the invention has reasonable structural design and has the following beneficial effects:
1) In the step 2, the preheating calandria plays two roles of withdrawing polymerization heat and preheating the mixture A, the polymerization heat is fully utilized, after the mixture A comes out of the preheating calandria, the mixture A enters a constant temperature heater for heating, then enters a static mixer for mixing with an initiator, finally enters an inner cavity of a polymerization reactor, the center of the inner cavity is a spiral propeller, the mixture A mixed with the initiator is subjected to bulk polymerization under the conditions of rapid stirring and heating temperature control, the rear section of the polymerization reactor is provided with strong heat exchange for controlling the highest temperature of the bulk polymerization, the highest temperature is prevented from being too high, the polymer has small molecular weight and wide distribution, and the polymer is oxidized and yellow due to the high temperature, and is cut into particles or cut into sections by a rotary cutter after being extruded from an outlet of the polymerization reactor, and then enters a curing reactor for continuous reaction and cooling, so as to obtain a polymer B;
2) The polymerization reactor in the second step consists of three sections, wherein the three sections are separated by a heat insulation gasket to reduce the mess of heat between the three sections of the metal inner cavity, and the first section of the inner cavity is an initiation section and has the heating and temperature control functions; the second section is a heat exchange section, one part of polymerization heat release causes the self-heating of materials to accelerate polymerization, and the other part of polymerization heat release is transferred to a mixture A in an outer wall preheating calandria; the third section is a strong heat exchange section, and has the main function of controlling the highest temperature of the bulk polymerization reaction to be between 96 and 135 ℃ and the retention time of materials in the inner cavity of the polymerization reactor to be between 32 and 150 seconds;
3) The preparation method of the continuous bulk polymerization high-absorptivity resin provided by the invention has the advantages of obvious energy consumption reduction and less carbon dioxide emission per ton of high-absorptivity resin products, and the appearance color, the centrifugal water retention rate and the pressurized absorptivity index can be kept equivalent. Not only can greatly reduce the energy consumption in the preparation process of the high-absorptivity resin, but also can simultaneously meet the technical index requirements of the high-absorptivity resin.
Drawings
FIG. 1 is a schematic structural view of a continuous bulk polymerized superabsorbent resin production system of the present invention.
FIG. 2 is a schematic diagram of the structure of the curing vessel of the present invention.
FIG. 3 is a schematic view showing the structure of the inside of the curing vessel of the present invention.
In the drawing the view of the figure,
1-preheating calandria inlet, 2-preheating calandria, 3-preheating calandria outlet, 4-heat insulation gasket, 5-constant temperature heater, 6-initiator addition, 7-static mixer, 8-spiral propeller, 9-motor, 10-initiation section heating temperature control, 11-polymerization reactor outlet, 12-rotary cutter, 13-strong cooling calandria unit, 14-initiation section, 15-heat exchange section, 16-strong heat exchange section 17-initiation section material temperature monitoring device, 18-heat exchange section material temperature monitoring device, 19-polymerization reactor outlet material temperature monitoring device, 20-preheating calandria inlet temperature monitoring device, 21-preheating calandria outlet temperature monitoring device, 22-constant temperature heater outlet temperature monitoring device, 23-polymerization reactor;
24-ripening device, 241-ripening device inlet, 242-ripening device outlet, 243-cooling air, 244-air cooling screen, 245-air cooling screen round holes, 246-ripening device rotary disc.
Detailed Description
The technical scheme of the invention is further described below with reference to the embodiment and the attached drawings.
The product performance test methods for the examples and comparative examples are as follows:
(1) Centrifugal water retention rate
The centrifugal retention rate (Centrifuge Retention Capacity, abbreviated as "CRC") refers to the water absorption retention rate after a unit mass of a highly absorbent resin has freely swelled in 0.9% sodium chloride brine for a certain period of time and a part of the water has been removed by a centrifuge.
Specifically, 0.2000G of a super absorbent resin was weighed by a tea bag, immersed in a 0.9wt% aqueous sodium chloride solution for 30 minutes to freely expand the resin, and then centrifuged to remove a part of the water by a centrifuge (centrifugal force: 250G) to maintain the water absorption rate (unit: G/G). Centrifuge retention = (m after centrifugation-m sample-m blank)/m sample.
(2) Absorption under pressure
The absorbency under pressure (Absorption Under Pressure, abbreviated as "AUP") refers to the water absorption capacity of a unit mass of a highly absorbent resin under a certain pressure for a certain period of time. Specifically, the water-absorbent resin was swollen with 0.9000g of a water-absorbent resin under a load of 0.7psi for 1 hour in a 0.9wt% aqueous sodium chloride solution, and the water-absorbent resin had a water absorption capacity (unit: g/g). Absorption under pressure= (m after water absorption-m before water absorption)/m samples.
The invention relates to a continuous mass polymerization high-absorptivity resin preparation system, which has the specific structure that: comprising the following steps:
a preheating gauntlet 2, a plurality of parallel and consecutively arranged preheating gauntlets 2, the preheating gauntlet 2 being used for preheating the mixture a;
the constant temperature heater 5 is communicated with the preheating calandria 2, and the preheated mixture A is subjected to temperature control through the constant temperature heater 5;
the static mixer 7, the static mixer 7 is communicated with discharge port of the constant temperature heater 5, one side of the static mixer 7 has initiator to add the mouth 6;
the polymerization reactor 23, the polymerization reactor 23 includes the reaction cavity, there are spiral thrusters 8 in the reaction cavity, one end of the spiral thrusters 8 has driving devices, the static mixer 7 is set up near one end of the driving device and communicated with polymerization reactor 23; the pitch of the helical propeller 8 increases gradually from the end closer to the drive means to the end further from the drive means.
Wherein, the reaction inner chamber of polymerization reactor 23 includes initiation section 14, heat exchange section 15, the strong heat exchange section 16 that set gradually, and the pitch of initiation section 14 is a, the pitch of heat exchange section 15 is b, the pitch of strong heat exchange section 16 is c, satisfies quantitative relation: a is less than b and less than c.
More specifically, the diameter of the inner cavity of the polymerization reactor 23 ranges from 305mm to 865mm, the polymerization reactor comprises an initiation section 14, a heat exchange section 15 and a strong heat exchange section 16 which are sequentially arranged, the length of the initiation section 14 ranges from 560mm to 2500mm, the screw pitch ranges from 52mm to 75mm, the length of the heat exchange section 15 ranges from 600mm to 2650mm, the screw pitch ranges from 95mm to 155mm, the length of the strong heat exchange section 16 ranges from 650mm to 2750mm, the screw pitch ranges from 95mm to 195mm, and the numerical values satisfy the number relation: a is less than b and less than c.
The screw pitch ratio of the screw of the initiating section 14 and the heat exchanging section 15 of the polymerization reactor is 1:1.2-1:2.2, and the screw pitch ratio of the screw of the initiating section 14 and the strong heat exchanging section 16 of the polymerization reactor is 1:1.2-1:2.2. The three sections of the initiation section 14, the heat exchange section 15 and the strong heat exchange section 16 of the reaction cavity of the polymerization reactor 23 are separated by heat insulation gaskets. The end of the polymerization reactor 23 is provided with a polymerization reactor outlet 11, and a rotary cutter 12 for cutting the polymer into pellets or into sections is provided at the polymerization reactor outlet 11.
More specifically, the three sections of outer cylinders are connected by using flanges, heat insulation gaskets are arranged between the flanges to prevent heat from being mixed and fleed between the three sections, the inner cavities of the polymerization reactor are communicated, the middle is provided with a spiral propeller, and materials are conveyed to an outlet through the inlet of the inner cavity by virtue of the spiral propeller.
A strong cooling gauntlet unit 13 is also provided at the outlet 11 of the polymerization reactor.
More specifically, the strong cooling calandria unit 13 realizes the strong cooling function of the strong heat exchange section of the polymerization reactor, is prepared by red copper materials with good heat transfer performance, and has a structure formed by encircling matrix annular calandria, and low-temperature refrigerating fluid circulates inside the calandria to realize the strong cooling function.
In the preparation system of the invention, the specific arrangement of the temperature control aspect is as follows: the initiation section 14 is provided with an initiation section heating temperature control 10; the material temperature monitoring device 17 of the initiation section is also arranged at the initiation section 14; the heat exchange section is provided with a heat exchange section material temperature monitoring device 18; the outlet of the polymerization reactor is provided with a material temperature monitoring device 19 at the outlet of the polymerization reactor; a preheating calandria inlet temperature monitoring device 20 is arranged at the inlet of the preheating calandria; a preheating calandria outlet temperature monitoring device 21 is arranged at the outlet of the preheating calandria; the outlet of the constant temperature heater is provided with a constant temperature heater outlet temperature monitoring device 22.
More specifically, the heating temperature control device 10 of the initiation section is provided with an electric heating component on the cylinder wall. The temperature monitoring corresponds to a temperature detection point, displays a temperature value, and meets the requirements of the process conditions on the temperature and the temperature difference range.
As shown in FIG. 2, the polymer cooling and conveying device further comprises a curing device 24, wherein a curing device inlet 241 and a curing device outlet 242 are formed in the curing device 24, a curing device rotating disc 246 and an air cooling screen 244 are arranged in the curing device 24, and the air cooling screen 244 cools and conveys the polymer under the driving of the curing device rotating disc 246. The air-cooled screen 244 is provided with through holes, which are round holes. The aperture of the round hole is 1.2-5.5 mm. The aperture ratio of the air-cooled screen 244 is 22% -41%.
The preparation system and the batching kettle adopt a continuous bulk polymerization method to prepare the high-absorptivity resin.
1) The preheating calandria has two functions of withdrawing polymerization heat and preheating the mixture A, fully utilizes the polymerization heat, after coming out of the preheating calandria, the mixture A enters a constant temperature heater for heating, then enters a static mixer for mixing with an initiator, finally enters an inner cavity of a polymerization reactor, the center of the inner cavity is a spiral propeller, the mixture A mixed with the initiator is subjected to bulk polymerization under the conditions of rapid stirring and heating temperature control, the rear section of the polymerization reactor is provided with strong heat exchange for controlling the highest temperature of the bulk polymerization, the highest temperature is prevented from being too high, the polymer molecular weight is prevented from being small and the distribution is wide, the polymer is extruded from an outlet of the polymerization reactor, and then subjected to rotary cutter dicing or cutting, and then enters a curing device for continuous reaction and cooling, so as to obtain a polymer B;
2) The polymerization reactor consists of three sections, the three sections are separated by a heat insulation gasket, so that the disordered channeling of heat between the three sections of the metal inner cavity is reduced, and the disordered channeling of heat between the three sections is not beneficial to the temperature control and energy consumption loss of each section. The first section of the polymerization reactor is an initiation section and has the heating and temperature control functions; the second section of the polymerization reactor is a heat exchange section, one part of polymerization heat release causes the self-heating of materials to accelerate polymerization, and the other part of polymerization heat release is transferred to a mixture A in an outer wall preheating calandria; the third section of the polymerization reactor is a strong heat exchange section, the main function is to control the highest temperature of bulk polymerization reaction to be 96-135 ℃, the retention time of materials in the inner cavity of the polymerization reactor to be 32-150 seconds, the screw pitch ratio of the screw of the initiation section and the screw of the heat exchange section of the polymerization reactor to be 1:1.2-1:2.2, the screw pitch ratio of the screw of the initiation section and the screw of the strong heat exchange section of the polymerization reactor to be 1:1.2-1:2.2, the polymerization reactor is designed into three sections, so as to realize chain initiation of free radical polymerization, namely the initiation is heated to form free radicals in the initial stage, the middle is a chain growth stage, the rate and the strength of the polymerization reaction are controlled by partial heat dissipation, and finally the termination of the polymerization reaction is controlled by strong heat exchange and cooling. The screw pitches of the initiation section, the heat exchange section and the strong heat exchange section of the polymerization reactor are different, so that the residence time of materials in each section of the polymerization reactor is controlled, when the screw propellers rotate at the same speed, the screw pitches are short, the residence time of the materials is long, the residence time of the materials is short, the screw pitches of the initiation section are short because of long time required for initiating a free radical polymerization chain slowly, and the screw pitches of the heat exchange section and the strong heat exchange section are short because of rapid growth and rapid chain termination of the free radical polymerization chain;
3) The curing device is in an air-cooled screen plate chain circulation type, the residence time of the materials in the curing device is controlled to be 1-6 minutes, and the temperature control range of the materials at the outlet of the curing device is 70-30 ℃, so that the two functions of complete polymerization and cooling are realized. The air-cooled screen plate is provided with round holes, the diameter of the round holes is 1.2-5.5 mm, and the aperture ratio (sum of all open areas on the screen plate and total area of the screen plate) of the air-cooled screen plate is 22% -41%. The size of the circular aperture cannot allow materials to leak out of the circular hole, and cold air penetration is ensured to cool. The aperture ratio of the air-cooled screen balances the penetration of cold air and the structural mechanics of the air-cooled screen.
Example 1:
adding 300kg of sodium acrylate and acrylic acid (the sodium acrylate accounts for 75% of mole fraction), 0.9kg of bifunctional cross-linking agent polyethylene glycol (600) diacrylate and 3kg of dispersing agent gas phase method silicon dioxide, 0.04kg of metal ion chelating agent ethylenediamine tetraacetic acid disodium salt into a batching kettle, stirring into a mixture A in the batching kettle, measuring the current temperature of the mixture A to be 22 ℃, feeding the mixture A into a preheating calandria of a specially-made polymerization reactor by a plunger pump according to the current temperature of 102kg/h, detecting the temperature of the mixture A from the outlet of the preheating calandria, heating the mixture A to be 43 ℃ in a constant temperature heater, mixing the mixture A with initiator sodium persulfate 0.32kg/h in a static mixer, feeding the mixture A into the cavity of the polymerization reactor, displaying the highest temperature of the cavity of the polymerization reactor to be 123 ℃, keeping the material in the cavity for 96 seconds, cutting particles in a rotating way from the outlet of the polymerization reactor, feeding the mixture A into a curing device for 2.1 minutes to obtain a polymer B at 52 ℃, and crushing or grinding, sieving and surface treating the polymer B to obtain a final product C.
Comparative example 1
Adding 300kg of sodium acrylate and acrylic acid (the sodium acrylate accounts for 75% of mole fraction), 0.9kg of bifunctional cross-linking agent polyethylene glycol (600) diacrylate and 3kg of dispersing agent gas phase method silicon dioxide, stirring 0.04kg of metal ion chelating agent ethylenediamine tetraacetic acid disodium salt into a mixture in a batching kettle, measuring the temperature of the mixture at the moment to be 22 ℃, pumping the mixture A into a constant temperature heater by a plunger pump in an amount of 102kg/h to be heated to 95 ℃, mixing the mixture A with an initiator sodium persulfate in a static mixer for 0.32kg/h, controlling the residence time of the mixture A in a polymerization reactor consisting of a section of screw propeller with equal pitch to 96 seconds, measuring the highest temperature of materials in the polymerization reactor to be 152 ℃, cutting particles (yellowing particles by a rotary cutter, leading polymerization inhibitor brought in acrylic acid to oxidize to yellow by the material temperature in the polymerization reactor), and obtaining a yellow polymer at 102 ℃ after the mixture A is put into a curing device for 2.1 minutes, and obtaining a final product after the polymer is crushed or ground, sieved and subjected to surface treatment.
Comparative example 2
Adding 300kg of sodium acrylate and acrylic acid (the sodium acrylate accounts for 75% of mole fraction), 301.2kg of deionized water and 0.9kg of N, N-methylene bisacrylamide into a batching kettle, starting stirring of the batching kettle, controlling the temperature to 82+/-2 ℃, conveying the mixture into a static mixer by using a pump at the temperature of 215kg/h, simultaneously adding 20.8kg of 1% sodium persulfate aqueous solution, entering a silica gel reactor of a circulating chain for polymerization reaction to obtain polymerized gel, and granulating, drying, crushing or grinding, screening and surface treating the polymerized gel to obtain a final product.
The superabsorbent resins obtained in example 1, comparative example 1 and comparative example 2 are detailed in table 1 below:
table 1 results of the performance tests of example 1, comparative example 2
As can be seen from the analysis of Table 1, the preparation method of the continuous bulk polymerization high-absorptivity resin provided by the invention has the advantages of obvious energy consumption reduction and low carbon dioxide emission per ton of high-absorptivity resin product, and the appearance color, the centrifugal water retention rate and the pressurized absorptivity index can be kept equivalent. Not only can greatly reduce the energy consumption in the preparation process of the high-absorptivity resin, but also can simultaneously meet the technical index requirements of the high-absorptivity resin.
The preferred embodiments of the present invention are described herein, but the scope of the present invention is not limited thereto. Modifications, additions, or substitutions of the described embodiments by those skilled in the art are intended to be within the scope of the present invention.
Claims (9)
1. A method for preparing a continuous mass polymerized superabsorbent resin, comprising:
step one: preparing a mixture A from vinyl monomers, salts thereof, cross-linking agents with more than two functional groups, dispersing agents and metal ion chelating agents;
step two: the mixture A is pumped into a feeding preheating calandria of a polymerization reactor through a plunger pump, and after coming out of the preheating calandria, the mixture A enters a constant temperature heater for heating, then enters a static mixer for mixing with an initiator, finally enters an inner cavity of the polymerization reactor, the center of the inner cavity is a spiral propeller, and the mixture A mixed with the initiator is subjected to bulk polymerization under the conditions of rapid stirring and heating temperature control;
step three: the polymer is extruded from the outlet of the polymerization reactor, then is cut into particles or segments by a rotary cutter, and enters a curing device for continuous reaction and cooling to obtain a polymer B;
step four: the polymer B is crushed or ground, screened and surface treated to obtain the final product C.
2. The method for producing a continuous bulk polymerized superabsorbent resin according to claim 1, characterized in that: the vinyl monomer and the salt thereof in the step one are selected from at least one of carboxylic acid group monomer and the salt thereof containing double bonds, sulfonic acid group monomer and the salt thereof, and phosphoric acid group monomer and the salt thereof.
3. The method for producing a continuous bulk polymerized superabsorbent resin according to claim 1, characterized in that: the temperature rise range of the mixture A from the inlet to the outlet of the preheating calandria in the second step is 8-32 ℃, and the temperature control range of the mixture A at the outlet of the constant temperature heater is 82-125 ℃.
4. The method for producing a continuous bulk polymerized superabsorbent resin according to claim 1, characterized in that: the polymerization reactor in the second step consists of three sections which are separated by heat-insulating gaskets.
5. The method for producing a continuous bulk polymerized superabsorbent resin according to claim 1, characterized in that: the first section of the inner cavity of the polymerization reactor is an initiating section, the second section is a heat exchange section, and the third section is a strong heat exchange section.
6. The method for producing a continuous bulk polymerized superabsorbent resin according to claim 1, characterized in that: the residence time of the material in the inner cavity of the polymerization reactor is 32-150 seconds.
7. The method for producing a continuous bulk polymerized superabsorbent resin according to claim 5, wherein: the screw pitch ratio of the screw of the initiation section and the heat exchange section of the polymerization reactor is 1:1.2-1:2.2, and the screw pitch ratio of the screw of the initiation section and the screw of the strong heat exchange section of the polymerization reactor is 1:1.2-1:2.2.
8. The method for producing a continuous bulk polymerized superabsorbent resin according to claim 1, characterized in that: the curing device in the third step is an air-cooled mesh plate chain circulation type, the residence time of the materials in the curing device is controlled to be 1-6 minutes, and the temperature control range of the materials at the outlet of the curing device is 70-30 ℃.
9. The method for producing a continuous bulk polymerized superabsorbent resin according to claim 8, wherein: the air-cooled screen plate is provided with round holes, the diameter of the round holes is 1.2-5.5 mm, and the aperture ratio of the air-cooled screen plate is 22-41%.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| KR20100078740A (en) * | 2008-12-30 | 2010-07-08 | 주식회사 엘지화학 | Continuous manufacturing methods of polymer |
| CN108671867A (en) * | 2018-06-06 | 2018-10-19 | 博立尔化工（扬州）有限公司 | A kind of device and method thereof preparing solid propenoic acid resin |
| CN213977502U (en) * | 2020-12-21 | 2021-08-17 | 山东友泉新材料有限公司 | Continuous production device of hydroxyl acrylic resin |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| KR20100078740A (en) * | 2008-12-30 | 2010-07-08 | 주식회사 엘지화학 | Continuous manufacturing methods of polymer |
| CN108671867A (en) * | 2018-06-06 | 2018-10-19 | 博立尔化工（扬州）有限公司 | A kind of device and method thereof preparing solid propenoic acid resin |
| CN213977502U (en) * | 2020-12-21 | 2021-08-17 | 山东友泉新材料有限公司 | Continuous production device of hydroxyl acrylic resin |
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