CN102731713A - Preparation method for high-performance absorbent resin - Google Patents
Preparation method for high-performance absorbent resin Download PDFInfo
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- CN102731713A CN102731713A CN2012102564758A CN201210256475A CN102731713A CN 102731713 A CN102731713 A CN 102731713A CN 2012102564758 A CN2012102564758 A CN 2012102564758A CN 201210256475 A CN201210256475 A CN 201210256475A CN 102731713 A CN102731713 A CN 102731713A
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Abstract
The invention relates to a preparation method for high-performance absorbent resin. The preparation method comprises the following steps that: (1) wide super-absorbent resin gel with the water content being 50wt% which is obtained by free radical polymerization reaction on a continuous cycle belt is pelleted and a redox initiator is added during gel pelleting; (2) after pelleting, the gel grains are evenly distributed on a circulating air belt-type machine for drying, the drying process is divided into three stages of drying constant speed stage, drying speed reduction stage and drying cooling stage and the temperature and the air speed of hot air of a drier are adjusted according to the change of the water content of the gel at different drying stages; and (3) the dried materials which are obtained are crushed, grinded and screened to obtain the grains with qualified grain diameter; the surface of the super-absorbent resin grains with qualified grain diameter is coated with a superficial cross-linking agent; and the grains are heated and an anti-yellowing assistant and a grain moisture-proof clustering agent are added during the process that the materials are cooled. The absorbent resin gel prepared by the method provided by the invention has excellent physical usability.
Description
Technical field
The present invention relates to a kind of preparation method of high-performance water-absorbing resin.
Background technology
Super absorbent resin (SAP) is since the seventies in 20th century development and the suitability for industrialized production, and the super absorbent resin that vinylformic acid and vinylformic acid salt thereof carry out the crosslinking polymerization gained is because of its raw material is easy to get, cheap for manufacturing cost, products obtained therefrom excellent performance becomes the present product that generalizes large-scale industrial production most.And be applied to paper diaper; The performance requriements of the super absorbent resin of health fields such as sanitary napkin has experienced three phases; From the initial simple saturated liquid absorption of stressing water-absorbing resin; To stressing the pressurization liquid absorption; So far requiring product to have low residual monomer amount, low water soluble, to go out thing, high pressurization liquid absorbency rate, uptake rate fast, more require simultaneously absorbent resin through the gel after the imbibition swelling have excellent liquid transmitting capacity and storageability (material depositing with use in anti-xanthochromia and anti-moisture absorption conglomeration performance).
Usually the polymer gel that obtains through polymerization must disclose the drying of polymkeric substance through super-dry in the 87-93 page or leaf of " modern high water absorbency polymer technology " monograph.Be the dry polymer gel, preferably use the force air conveyor dryer, institute's exsiccant material water-content is preferably 1-5%.
The preparation method of the low water-absorbing polymeric particles of residual monomer content has been described among the EP289 338A1.In the drying of polymer gel, use air through the HP steam heating, the HP steam that adds warm air that under closed-loop control, will flow into through the part cycle gas is adjusted to desirable value.
For improving the hydraulic permeability of product swell gel after pick up under the high capacity and imbibition, preferably dried particle is pulverized, to obtain to reach the particle of qualified size distribution, carry out the surface-crosslinked reaction of particulate then.For example: CN1616525A (day touches), CN 1715302A (University Of Suzhou), CN1475517A (day touches).Though the SAP resin after surface-crosslinked obviously improves at the liquid absorbency rate under the load, the gel liquid transmitting capacity after the imbibition swelling is not improved.In CN101531728 (Shandong); CN1856331A (BASF); After surface-crosslinked the processing or in surface-crosslinked reaction process, adding the auxiliary agent that improves gel brine stream conductance at the SAP particle surface, the auxiliary agent that is added can be polyvalent metal salt class or inorganic powder class.
Above process method can not be improved each item performance requriements of present health field for super absorbent resin all sidedly.Adopt process production techniques of the present invention; Can realize more all sidedly that the low remaining Acrylic Acid Monomer of absorbent resin product, low water soluble go out thing, gel liquid perviousness and powder granule have each item performances such as good anti-xanthochromia and damp proof conglomeration property after high-liquid absorbing rate under the load and the imbibition in put procedure.
The present invention mainly is achieved through the following step: 1) will be on continuous tape loop obtaining water cut with the Raolical polymerizable mode is that the high water absorbent resin gel of 50% wide cut carries out granulation, in the gel granulation process, adds redox initiator solution; Then that this granulation is good gel particle is distributed to the travelling belt of recirculated air belt machine through a hydraulic pressure swing material distributing machine; Before carrying out drying; Through a screeder the transversely uniform thickness ground of gel masses at travelling belt is distributed, thereby make gel masses evenly to carry out drying at three follow-up drying stages (dry constant-speed section, dry reduction of speed section, cooling section) effectively.Through regulating air intake hot blast temperature, the intake velocity of dry three phases; With each section desiccant gel water-content; Make gel particle fully react, thereby remaining Acrylic Acid Monomer content and water soluble apparent extract in the dried particles of final acquisition are minimized at the monomer that dry constant-speed section can not have polymerization stage initiator complete reaction and that in the gel granulation process, add and polymerization left behind; And under the condition of the high temperature of dry reduction of speed section, high wind speed, the aqueous gel particle is carried out drying apace, reach the required more excellent particle water cut (5-8%) of follow-up pulverizing ground section.Be cooled to follow-up pulverizing through the qualified SAP particle of dry reduction of speed section water cut at dry cooling section and grind required temperature of charge (50-80 ℃).Thus obtained dried material obtains the super absorbent resin particle of qualified particle diameter through follow-up pulverizing, grinding, screening; Having the super absorbent resin particle surface coated surface linking agent of qualified particle diameter, carry out heat treated then, thereby in the material process of cooling, add the super absorbent resin product of each item excellent performance that color stabilizer and the damp proof conglomeration agent of particle obtain.
Summary of the invention
The purpose of this invention is to provide a kind of method of manufacture, for the super absorbent resin of realizing manufacturing has excellent each item over-all properties (low residual monomer content, low water soluble go out thing, high capacity pick up, hydraulic permeability that the imbibition swell gel is high etc.) with high performance absorbent resin.
A kind of preparation method of high-performance water-absorbing resin is characterized in that: this method comprises the steps:
(1) will be that the high water absorbent resin gel of 50wt% wide cut carries out granulation through on continuous tape loop, obtaining water cut, in the gel granulation process, add oxidation, reduction initiator with the Raolical polymerizable mode;
(2) gel particle that is 55wt% with the good water cut of granulation is uniformly distributed into and carries out drying on the recirculated air belt machine; This drying process was divided into for three stages; That is: dry constant-speed section, dry reduction of speed section and dry cooling section; According to the changing conditions of different drying stage gel water cut, regulate the inlet air temperature of drying machine warm air and the inflow velocity of warm air;
(3) qualified particle diameter is pulverized, grinds, sieved out to resulting dried material, qualified grain diameter is 100-850 μ m; After having the super absorbent resin particle surface coated surface linking agent of qualified particle diameter, carry out heat treated, in the material process of cooling, add anti-yellowing additive and the damp proof conglomeration agent of particle.
In the step of the present invention (1) in the gel granulation process oxidation initiator addition be the 10-200ppm of gel weight, reduction initiator addition is the 20-200ppm of gel weight.
The surface crosslinking agent that particle surface applies in the step of the present invention (3) is selected from one or more in diglycidylether, alkylene carbonate or the polyvalent alcohol, and its addition is 0.01wt%-2.0wt%; Its surface-crosslinked temperature of reaction is 100-210 ℃, and the reaction times is 20-90min.
Be uniformly distributed on the recirculated air conveyor dryer through a hydraulic pressure swing material distributing machine through the good gel particle of granulation in the step of the present invention (2); And then the gel particle fabric thickness on request that will be distributed on the drying machine travelling belt through a screeder is evenly distributed on the travelling belt, and the gel thicknesses on the drying machine travelling belt is 70-100mm.
In the step of the present invention (2) at different drying stages, the test of desiccant gel particle water cut be through continuously at sampling spot, in specific time spacer, carry out sample circuit test, get the sample analysis result five times, deviation≤2 weight %.
Dry constant-speed section is divided into 1-3 district in the step of the present invention (2); Cut off by the stainless steel heavy curtain between each district; Gel water cut when dry constant-speed section is accomplished is controlled to be 20-35 weight %; Its temperature of passing the heated drying air behind the gel particle layer is controlled at 70-150 ℃, and the speed control that warm air flows into is 10-20min at 0.2-2.0m/s in the dry constant-speed section residence time.
Dry reduction of speed section is divided into 2-3 district in the step of the present invention (2); Cut off by the stainless steel heavy curtain between each district; The water cut of dried particles is 5-8 weight % when dry reduction of speed section is accomplished; The temperature of passing the heated drying air after material bed is controlled at 150-180 ℃, and the speed control that warm air flows into is 10-20min at 1.0-5.0m/s in the dry reduction of speed section residence time.
Dry cooling section uses a district in the step of the present invention (2); Discharging material moisture through cooling after drying machine is 2-8 weight %; Drop temperature is controlled at 50-80 ℃, and the speed control that freezing air flows into is 3-10min at 1.0-5.0m/s in the residence time of cooling section.
The coated surface linking agent is carried out on qualified size particles surface through super-dry, pulverizing, screening obtain; And through surface-crosslinked reacted high-performance water-absorbing resin (SAP) granule materials; In process of cooling, add anti-yellowing additive and damp proof conglomeration agent; Anti-yellowing additive wherein is selected from one or more in lime carbonate, sodium sulfate (magnesium), titanium oxide, Vanadium Pentoxide in FLAKES, 2-hydroxyl-2-sulfino acetate disodium salt, quadrol, tetren, the penten, and its addition is 0.1-3.0wt%; Damp proof conglomeration agent is selected from one or more in zeyssatite, silicon-dioxide, Tai-Ace S 150, sodium lauryl sulphate, polyoxyethylene laurel ether, the Voranol EP 2001, and its addition is 0.1-3.0wt%.
< 100ppm, water soluble go out thing < 10 weight % through its remaining Acrylic Acid Monomer amount of the prepared absorbent resin of the present invention; 0.7psi the suction salt solution multiplying power under the load can 18g/>g; < product of each item excellent combination property such as 30s, it can be widely used in the health field gel permeation after the imbibition.And ME of the present invention is simple, is applicable to suitability for industrialized production.
Embodiment
The test of prepared in the present invention absorbent resin each item performance is implemented as follows:
1. remaining Acrylic Acid Monomer content in the product:
Get 0.5g absorbent resin sample, place the saline water of 100ml, stir after 0.5 hour; Placed 24 hours; Then the swollen resin is filtered, collect and the filtrating of the gained of weighing, filtrating is carried out liquid-phase chromatographic analysis; According to the peak area that is obtained, filtrating quality and the vinylformic acid standardized solution curve demarcated in advance, calculate the content of remaining Acrylic Acid Monomer in institute's test sample article then.
2. water soluble apparent extract in the product:
In the 250mL beaker, the weighing 184.3g0.9wt%NaCl aqueous solution joins the 1.00gSAP sample in this solution, stirs 16h with the soluble component of extraction in the SAP sample.The solution of this extraction is filtered with filter paper, and weighing 50.0g gained filtrating is as measuring filtrating.At first, carry out the titration of blank solution (aqueous solution of 0.9wt% NaCl), use the 0.1mol/LNaOH aqueous solution to carry out titration, up to pH=10; Through using the titration of 0.1mol/L hydrochloric acid soln,, obtain the blank titration amount and be respectively [bNaOH], [bHCl] mL subsequently up to pH=2.7.Sample extraction liquid is carried out above-mentioned same titration operation, obtain titer and be respectively [NaOH], [HCl] mL.The soluble component content Ex of SAP sample and degree of neutralization DN can be by computes, wherein M
wBe molecular-weight average.
3. the pick up of product under the load:
It is that 25mm has in the sieve right cylinder at the end that the 0.2g sample is placed on internal diameter, and sample is applied the load of 0.7psi, then this right cylinder is placed the petridish of (± 2 ℃) saline water that has 25 ℃, lets it inhale saline water 1 hour, surveys its liquid absorption then.
4. the hydraulic permeability of product after the imbibition swelling
Taking by weighing the 0.32g specimen is positioned over and stirs in the saline water of 150g and left standstill swelling 30 minutes, preparation aqueous gel particle.The embolism of dead front type chromatographic column that will have the strainer of embolism and containing mark is closed, and this embolism is made as downside and vertically fixing this chromatographic column.Flow through freely leading to the liquid time of fluid-through tube with saline water under the saline water blank testing situation of 25 ℃ (± 2 ℃); Write down and be T1; Aqueous gel particle for preparing and saline water are transferred in the chromatographic column together, and with the pressuring shaft of the circular metal silk screen that at one end vertically has sieve aperture, the mode that is positioned at aqueous gel particle one side according to wire cloth is put into; Place weight again and leave standstill and opened the fluid-through tube bottom valve in 1 minute, write down the flow through time T 2 of fluid-through tube of saline water.Required time is few more, and then the hydraulic permeability of product imbibition gel is good more.The hydraulic permeability of product is: T2-T1,
5. the mensuration of moisture absorption caking rate
2.00g is dispersed evenly to the cup end of the plastic cup of bottom surface diameter 50mm, height 11mm as the absorbent resin of 850 μ m screen underflows or water absorbency resin composition; Put into fast in the climatic chamber that is adjusted into 25 ℃ of temperature, relative humidity 90RH% in advance, placed 1 hour.Thereafter; Absorbent resin after the moisture absorption or water absorbency resin composition are moved in the JIS standard sieve of diameter 7.5cm, mesh 200 μ m; Utilize sieve shaker) sieved 5 minutes; Mensuration residues in the weight of absorbent resin or water absorbency resin composition on the sieve and through the absorbent resin of sieve or the weight of water absorbency resin composition, respectively as being W1 (g) and W2 (g).Then, go out the moisture absorption caking rate by these weight (W1 and W2) according to computes.In addition, adopt the value of the MV of 5 mensuration as the moisture absorption caking rate of test sample, the moisture absorption caking rate is low more, means that the moisture absorption flowability is more excellent.Moisture absorption caking rate [%]=W1/ (W1+W2) * 100
The sample yellowing resistance can:
Sample is filled up magazine, and specimen whiteness H1 puts into sample in the climatic chamber that is adjusted into 60 ℃ of temperature, relative humidity 90RH% in advance then, and after 21 days, the whiteness H2 of specimen calculates its yellowing resistance then.Anti-xanthochromia rate [%]=(H1-H2)/H1*100 numerical value is more little, explains that its yellowing resistance is good more.
Embodiment
The preparation of polymeric gel:
It is 38 weight % that the acrylic acid solution of polyoxyethylene glycol-200 diacrylate of the sodium hydroxide solution through continuous mixing water, 32 weight %, vinylformic acid, 20 weight % makes solid content; Degree of neutralization is 75% polymerization single polymerization monomer solution; This polymerization single polymerization monomer solution is cooled to temperature about 60 ℃ through an interchanger, in this polymerization single polymerization monomer solution, adds the ammonium persulfate aqueous solution of 3wt% and the sodium sulfite anhy 96 of 1wt% then, after mixing; Be supplied to circulation belt polymerization reactor to carry out polymerization reactor apace; Material residence time in polymerization reactor is about 20min, thereby obtains 550kg/h, and water cut is about 50%; Wide cut is 600mm, and thickness is the polymeric gel of 20mm.
This polymeric gel is cut apart through vertical, horizontal cutting knife; Carry out the gel granulation at a screw extrusion press then, in granulation process, add the ammonium persulfate aqueous solution of 0.3wt% and the aqueous solution of sodium bisulfite of 0.1wt%; Addition is about 5% of a gel content; Finally obtain 600-620kg/h, water cut is about 55wt%, and particle size is the gel particle about 10-20mm; This gel granulation is uniformly distributed into through hydraulic pressure swing material distributing machine and rake formula screeder carries out drying on the forced hot air circulation conveyor dryer, material bed thickness is 80mm.
Embodiment 1
Drying conditions is: dry constant-speed section is divided 2 districts, and the HAI Heated Air Intake temperature is 150-160 ℃, and passing material bed temperature is 70-150 ℃, and gas flow rate is 1m/s, and the gel particle water cut that goes out constant-speed section is about 30wt%, is 15min in the residence time of constant-speed section; Dry reduction of speed section also is divided into 2 districts, and the HAI Heated Air Intake temperature is 160-180 ℃, and passing material bed temperature is 150-180 ℃; Gas flow rate is 3m/s, and the gel particle water cut that goes out the reduction of speed section is about 6wt%, and material is 15min in the residence time of reduction of speed section; Dried material entering cooling area carries out the cooling of dried material then, and this section temperature is 50～80 ℃, and the cooling gas flow velocity is 3m/s; This section residence time is 5 minutes, is 5wt% through the 3rd step cooling after drying particulate water cut.
The particle that above-mentioned drying is obtained through pulverize, to obtain the average grain particle diameter be 380 μ m particles to sub-sieve; This particle is carried out surface crosslinking agent to apply and reacting by heating; Surface crosslinking agent is the mixture of glycerine, terepthaloyl moietie and the water of 15 weight %; Its three's ratio is 2:1:7, and the reacting by heating temperature is 190 ℃, and the reaction times is 45min.To cool off through surface-crosslinked reacted particle subsequently; When being cooled to 80 ℃ of left and right sides; Add the silicon-dioxide (particle < 20 μ m) and the 2 weight % sodium ethylene diamine tetracetate aqueous solution (100ppm) of 1.0 weight %, the absorbent resin product performance that finally obtain are seen table 1
Embodiment 2
Drying conditions such as embodiment 1, the gas flow rate that changes dry constant-speed section are 15min to 2.0m/s in the residence time of constant-speed section; The gel particle water cut that goes out constant-speed section is about 20wt%; The hot blast temperature and the gas flow rate of dry reduction of speed section do not change; In the gel particle water cut that goes out the reduction of speed section is about 4%, and the condition of dry cooling section is 3wt% also like example 1 through cooling after drying particulate water cut.
The particle that above-mentioned drying is obtained through pulverize, to obtain the average grain particle diameter be 380 μ m particles to sub-sieve; Resulting granules is carried out particle surface like example 1 to be handled; At particle through surface-crosslinked reaction cooled to 70 ℃; Add the Tai-Ace S 150 particle (particle < 100 μ m) of 1.0 weight % and the T 46155 octadecoic acid natrium aqueous solution (200ppm) of 2 weight %.The absorbent resin product performance that finally obtain are seen table 1
Comparative Examples 1
Drying conditions is: dry constant-speed section is divided 2 districts; The HAI Heated Air Intake temperature is 150-160 ℃, and passing material bed temperature is 120-150 ℃, and gas flow rate is 3m/s; The gel particle water cut that goes out constant-speed section is about 10wt%, is 15min in the residence time of constant-speed section; Dry reduction of speed section also is divided into 2 districts, and the HAI Heated Air Intake temperature is 160-180 ℃, and passing material bed temperature is 150-180 ℃; Gas flow rate is 3m/s, and the gel particle water cut that goes out the reduction of speed section is about 2wt%, and material is 15min in the residence time of reduction of speed section; Dried material entering cooling area carries out the cooling of dried material then, and this section temperature is 50～80 ℃, and the cooling gas flow velocity is 3m/s; This section residence time is 5 minutes, is 2% through cooling after drying particulate water cut.
The particle that above-mentioned drying is obtained through pulverize, to obtain the average grain particle diameter be 380 μ m particles to sub-sieve; This particle is carried out particle surface crosslinking reaction and the aftertreatment of particle in process of cooling by the method for embodiment 1, and the absorbent resin product performance that obtain are seen table 1
Comparative Examples 2
Carry out gel particle drying, pulverizing, sub-sieve and particle surface crosslinking reaction like the method for embodiment 1, in the particle process of cooling, add the T 46155 octadecoic acid natrium aqueous solution (200ppm) of 2 weight %, the product performance that preparation reaches are seen table 1
Comparative Examples 3
Carry out gel particle drying, pulverizing, sub-sieve and particle surface crosslinking reaction like the method for embodiment 1, in the particle process of cooling, add the diethylidene pentaacetic acid sodium water solution of 2 weight %, the product performance that preparation reaches are seen table 1
The result shows; In institute of the present invention research range; The drying conditions of gel particle is for the residual monomer content of the finished product, and pick up under water soluble apparent extract, the load and gel permeation are all influential, and in process of cooling; The interpolation of anti-moisture absorption conglomeration agent and anti-yellowing additive is for the gel permeation of the finished product; The influence of anti-moisture absorption conglomeration property of product and yellowing resistance is very big, so adopt method of manufacture of the present invention, can prepare all excellent product of each item physics and use properties.
Claims (10)
1. the preparation method of a high-performance water-absorbing resin, it is characterized in that: this method comprises the steps:
(1) will be that the high water absorbent resin gel of 50wt% wide cut carries out granulation through on continuous tape loop, obtaining water cut, in the gel granulation process, add oxidation, reduction initiator with the Raolical polymerizable mode;
(2) gel particle that is 55wt% with the good water cut of granulation is uniformly distributed into and carries out drying on the recirculated air belt machine; This drying process was divided into for three stages; That is: dry constant-speed section, dry reduction of speed section and dry cooling section; According to the changing conditions of different drying stage gel water cut, regulate the inlet air temperature of drying machine warm air and the inflow velocity of warm air;
(3) qualified particle diameter is pulverized, grinds, sieved out to resulting dried material, qualified grain diameter is 100-850 μ m; After having the super absorbent resin particle surface coated surface linking agent of qualified particle diameter, carry out heat treated, in the material process of cooling, add anti-yellowing additive and the damp proof conglomeration agent of particle.
2. method according to claim 1 is characterized in that: in the step (1) in the gel granulation process oxidation initiator addition be the 10-200ppm of gel weight, reduction initiator addition is the 20-200ppm of gel weight.
3. method according to claim 1 is characterized in that: the surface crosslinking agent that particle surface applies in the step (3) is selected from one or more in diglycidylether, alkylene carbonate or the polyvalent alcohol, and its addition is 0.01wt%-2.0wt%; Its surface-crosslinked temperature of reaction is 100-210 ℃, and the reaction times is 20-90min.
4. method according to claim 1; It is characterized in that: be uniformly distributed on the recirculated air conveyor dryer through a hydraulic pressure swing material distributing machine through the good gel particle of granulation in the step (2); And then the gel particle fabric thickness on request that will be distributed on the drying machine travelling belt through a screeder is evenly distributed on the travelling belt, and the gel thicknesses on the drying machine travelling belt is 70-100mm.
5. method according to claim 1; It is characterized in that: in the step (2) at different drying stages; The test of desiccant gel particle water cut be through continuously at sampling spot, in specific time spacer, carry out sample circuit test, get the sample analysis result five times, deviation≤2 weight %.
6. according to claim 1; 5 described methods is characterized in that: dry constant-speed section is divided into 1-3 district in the step (2), is cut off by the stainless steel heavy curtain between each district; Gel water cut when dry constant-speed section is accomplished is controlled to be 20-35 weight %; Its temperature of passing the heated drying air behind the gel particle layer is controlled at 70-150 ℃, and the speed control that warm air flows into is 10-20min at 0.2-2.0m/s in the dry constant-speed section residence time.
7. according to claim 1; 5 described methods is characterized in that: dry reduction of speed section is divided into 2-3 district in the step (2), is cut off by the stainless steel heavy curtain between each district; The water cut of dried particles is 5-8 weight % when dry reduction of speed section is accomplished; The temperature of passing the heated drying air after material bed is controlled at 150-180 ℃, and the speed control that warm air flows into is 10-20min at 1.0-5.0m/s in the dry reduction of speed section residence time.
8. according to claim 1; 5 described methods; It is characterized in that: dry cooling section uses a district in the step (2), is 2-8 weight % through the discharging material moisture that cools off the after drying machine, and drop temperature is controlled at 50-80 ℃; The speed control that freezing air flows into is 3-10min at 1.0-5.0m/s in the residence time of cooling section.
9. according to the described method of claim 1-5; It is characterized in that: the coated surface linking agent is carried out on the qualified size particles surface through super-dry, pulverizing, screening obtain; And through surface-crosslinked reacted high-performance water-absorbing resin granule materials; In process of cooling, add anti-yellowing additive and damp proof conglomeration agent; Anti-yellowing additive wherein is selected from one or more in lime carbonate, sodium sulfate (magnesium), titanium oxide, Vanadium Pentoxide in FLAKES, 2-hydroxyl-2-sulfino acetate disodium salt, quadrol, tetren, the penten, and its addition is 0.1-3.0wt%; Damp proof conglomeration agent is selected from one or more in zeyssatite, silicon-dioxide, Tai-Ace S 150, sodium lauryl sulphate, polyoxyethylene laurel ether, the Voranol EP 2001, and its addition is 0.1-3.0wt%.
10. according to claim 1 or 8 described methods; It is characterized in that: < 100ppm, water soluble go out thing < 10 weight % to its remaining Acrylic Acid Monomer amount of prepared absorbent resin; 0.7psi the suction salt solution multiplying power under the load can 18g/>g, gel permeation < 30s after the imbibition.
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| CN103214616A (en) * | 2013-04-16 | 2013-07-24 | 华南理工大学 | Preparation method of porous-super-absorbent resin |
| CN104672479A (en) * | 2013-12-02 | 2015-06-03 | 上海华谊新材料有限公司 | High-water-absorptivity resin and preparation method thereof |
| CN105884974A (en) * | 2016-06-14 | 2016-08-24 | 四川省农业科学院生物技术核技术研究所 | Segmented drying method for starch system water-absorbent resin |
| CN109199701A (en) * | 2016-09-10 | 2019-01-15 | 山东诺尔生物科技有限公司 | A kind of composite absorption core and its application with imbibition self-expanding liquid-conveying ducts |
| CN109280185A (en) * | 2018-08-16 | 2019-01-29 | 仲恺农业工程学院 | A kind of high hydroscopic resin superfine powder surface modifying method and modification liquid |
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| CN103214616B (en) * | 2013-04-16 | 2015-09-02 | 华南理工大学 | A kind of preparation method of porous-super-absorberesin resin |
| CN104672479A (en) * | 2013-12-02 | 2015-06-03 | 上海华谊新材料有限公司 | High-water-absorptivity resin and preparation method thereof |
| CN105884974A (en) * | 2016-06-14 | 2016-08-24 | 四川省农业科学院生物技术核技术研究所 | Segmented drying method for starch system water-absorbent resin |
| CN105884974B (en) * | 2016-06-14 | 2018-07-13 | 四川省农业科学院生物技术核技术研究所 | A kind of starch-series water-absorbing resin stage drying method |
| CN109199701A (en) * | 2016-09-10 | 2019-01-15 | 山东诺尔生物科技有限公司 | A kind of composite absorption core and its application with imbibition self-expanding liquid-conveying ducts |
| CN109199701B (en) * | 2016-09-10 | 2022-02-01 | 山东诺尔生物科技有限公司 | Composite absorption core body with liquid-absorbing self-expanding liquid guide channel and application thereof |
| CN109280185A (en) * | 2018-08-16 | 2019-01-29 | 仲恺农业工程学院 | A kind of high hydroscopic resin superfine powder surface modifying method and modification liquid |
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| CN102731713B (en) | 2014-12-03 |
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Effective date of registration: 20170122 Address after: 201424 Fengxian District Cang Road, lane, Lane 357, room 100, room 295 Patentee after: Shanghai Hua Yi new material Co., Ltd Address before: 200137 Pudong North Road, Shanghai, No. 2031, No. Patentee before: Shanghai Huayi Acrylic Acid Co., Ltd. |