WO2004078796A1 - 吸水性樹脂の製造方法およびこれに用いられる乾燥装置 - Google Patents
吸水性樹脂の製造方法およびこれに用いられる乾燥装置 Download PDFInfo
- Publication number
- WO2004078796A1 WO2004078796A1 PCT/JP2004/002328 JP2004002328W WO2004078796A1 WO 2004078796 A1 WO2004078796 A1 WO 2004078796A1 JP 2004002328 W JP2004002328 W JP 2004002328W WO 2004078796 A1 WO2004078796 A1 WO 2004078796A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- water
- absorbent resin
- drying
- end wall
- stirring means
- Prior art date
Links
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/20—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
- B01F27/60—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a horizontal or inclined axis
- B01F27/72—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a horizontal or inclined axis with helices or sections of helices
- B01F27/726—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a horizontal or inclined axis with helices or sections of helices with two helices with opposite pitch on the same shaft; with two helices on the same axis, driven in opposite directions or at different speeds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles
- B01J8/10—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles moved by stirrers or by rotary drums or rotary receptacles or endless belts
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F2/00—Processes of polymerisation
- C08F2/32—Polymerisation in water-in-oil emulsions
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F6/00—Post-polymerisation treatments
- C08F6/14—Treatment of polymer emulsions
- C08F6/20—Concentration
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F6/00—Post-polymerisation treatments
- C08F6/24—Treatment of polymer suspensions
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F26—DRYING
- F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
- F26B11/00—Machines or apparatus for drying solid materials or objects with movement which is non-progressive
- F26B11/12—Machines or apparatus for drying solid materials or objects with movement which is non-progressive in stationary drums or other mainly-closed receptacles with moving stirring devices
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F26—DRYING
- F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
- F26B17/00—Machines or apparatus for drying materials in loose, plastic, or fluidised form, e.g. granules, staple fibres, with progressive movement
- F26B17/18—Machines or apparatus for drying materials in loose, plastic, or fluidised form, e.g. granules, staple fibres, with progressive movement with movement performed by rotating helical blades or other rotary conveyors which may be heated moving materials in stationary chambers, e.g. troughs
- F26B17/20—Machines or apparatus for drying materials in loose, plastic, or fluidised form, e.g. granules, staple fibres, with progressive movement with movement performed by rotating helical blades or other rotary conveyors which may be heated moving materials in stationary chambers, e.g. troughs the axis of rotation being horizontal or slightly inclined
Definitions
- the present invention relates to a method for producing a water-absorbent resin and a drying apparatus used for the method.
- the present invention relates to a method for producing a water-absorbent resin including a polymerization step by a reversed-phase suspension polymerization method and a subsequent drying step, and a drying apparatus used in the production method.
- the water absorbing resin is generally a lightly crosslinked polymer compound.
- Examples of the water absorbing resin include carboxymethyl cellulose, polyethylene oxide, a hydrolyzate of starch-acrylonitrile graft copolymer, polyacrylate, and vinyl alcohol-monoacrylate copolymer.
- Crosslinked products are known.
- FIG. 6 shows a conventional method for producing such a water absorbent resin.
- the conventional method for producing a water-absorbent resin includes a polymerization step S61, a dehydration step S62, and a desolvation step S63.
- a polymerization reaction is performed in a reaction tank 64 by a reversed-phase suspension polymerization method to produce a water-absorbing resin.
- the polymerization reaction is carried out in a state where an aqueous solution containing a predetermined water-soluble monomer for forming a resin and a radical polymerization initiator is suspended and dispersed in a hydrophobic solvent together with a surfactant.
- the surfactant is for stabilizing the dispersed aqueous solution of the monomer, and the hydrophobic solvent used is one that does not dissolve the monomer or the produced polymer.
- the water-absorbent resin generated through the polymerization step S61 is supplied to the next dehydration step S62 in a slurry state.
- a predetermined amount of the water-absorbent resin-containing slurry is Water is removed. Specifically, first, water and the solvent in the slurry are distilled off from the slurry under normal pressure, and collected by being condensed in the condenser 66.
- the condensed liquid is transferred from the condenser 66 to the separator 67, and then allowed to stand, whereby water and the solvent are separated.
- the solvent separated from the water is returned to the dehydration tank 65 in order to appropriately maintain the viscosity of the water-absorbent resin-containing slurry to be dehydrated in the dehydration tank 65.
- water is discharged outside the device.
- the water-absorbent resin-containing slurry that has been subjected to such dehydration treatment is then subjected to a solvent removal step S63.
- the water-absorbent resin is dried by desolvation dry ⁇ 68. Specifically, the solvent and remaining water in the slurry are distilled off from the slurry under normal pressure and collected in the condenser 69.
- the process for reducing only the water content of the slurry (dehydration step S62) is mainly performed by removing the solvent. Is carried out before the step of drying (desolvation step S63).
- the present invention was conceived under such circumstances, and it is an object of the present invention to provide a method for producing a water-absorbent resin with low energy and a drying apparatus used in the method. I do.
- a method for producing a water absorbent resin includes a polymerization step for producing a water-absorbent resin by a reversed-phase suspension polymerization method, and a drying step for drying the water-absorbent resin obtained in the polymerization step.
- a first stirring means provided on the rotating shaft for stirring the water-absorbent resin; and a first stirring means for stirring the water-absorbent resin while moving in a direction from the second end wall to the first end wall.
- the water-absorbent resin is dried by using a drying device comprising: a second stirring means provided on the rotating shaft between the stirring means and the second end wall.
- a polymerization step and a subsequent drying step are performed.
- a water-absorbent resin is generated by a reversed-phase suspension polymerization method, and the water-absorbent resin is contained or dispersed in a slurry and obtained in a state having a high water content.
- a drying apparatus having the above-described configuration is used, and the slurry is dried while being stirred in the apparatus. Specifically, the slurry is put into a device tank defined by the peripheral wall and the two end walls, and then the rotating shaft is rotated to thereby attach the slurry to the first end wall side of the shaft.
- the slurry or the highly water-absorbent resin is stirred by the stirring means and the second stirring means attached to the second end wall.
- the first stirring means stirs the water absorbent resin while moving the water absorbent resin in the direction from the first end wall to the second end wall.
- the second stirring means stirs the water absorbent resin while moving the water absorbent resin in the direction from the second end wall to the first end wall.
- a sufficient amount of water can be distilled off from the slurry together with the solvent in the drying step without clumping and unduly crushing. It is not necessary to perform the dehydration step involving reflux of the solvent having a relatively large energy loss, as described above with respect to. Therefore, according to the method of the first aspect of the present invention, it is possible to produce a water-absorbing resin with lower energy than, for example, the above-described conventional method.
- the drying device further includes a third stirring means for moving the water-absorbing resin in a rotating direction of the rotating shaft.
- the first stirring means stirs the water-absorbent resin while moving the water-absorbent resin in the direction from the first end wall to the second end wall.
- the stirring means stirs the water-absorbent resin while moving the water-absorbent resin in the direction from the second end wall to the first end wall.
- Move the water absorbent resin is suitable for imparting an appropriate rotational movement around the rotation axis to the slurry which is subjected to a drying operation in the drying apparatus! is there.
- the first stirring means and / or the second stirring means is preferably a ribbon screw.
- the ribbon screw is suitable as first and second stirring means for generating a counter flow.
- the peripheral speed of the first stirring means and the peripheral edge of the Z or second stirring means is preferably 1 m / s or less, more preferably 0.3 to 0.7 m / s.
- the peripheral speed of the third stirring means is preferably 0.3 m / s or more.
- the peripheral end speed is preferably 0.7 m / s or less.
- the distance between the peripheral end of the first stirring means and the Z or second stirring means and the peripheral wall is preferably 1 to 20 mm, more preferably 3 to 15 mm.
- the distance between the peripheral end of the third stirring means and the peripheral wall is set to the above range instead of the distance between the peripheral end of the first and second stirring means and the peripheral wall. It is preferable to set. From the viewpoint of suppressing lump and crushing of the water-absorbing resin while securing the drying efficiency, the separation distance is preferably in such a range.
- the pressure inside the drying device in the drying process is preferably 5 to:! OOkPa, and more preferably 20 to 70 kPa.
- the temperature inside the drying device in the drying step is preferably 60 to 100 from the viewpoint of shortening the drying time or suppressing the decomposition of the water-absorbent resin by heating. . C, more preferably 80 to 90 ° C.
- the water-absorbing resin contains a water-soluble ethylenically unsaturated monomer as a constituent.
- a polymer compound obtained by polymerizing a water-soluble ethylenically unsaturated monomer is suitable as a water-absorbing resin.
- an apparatus for drying a water-absorbent resin produced by a reversed-phase suspension polymerization method comprises a first end wall, a second end wall facing the first end wall, a peripheral wall and a rotating shaft extending between the two end walls, and a moving member which moves in a direction from the first end wall to the second end wall.
- First stirring means provided on the rotating shaft for stirring the water-absorbent resin, and first stirring for stirring the water-absorbent resin while moving in a direction from the second end wall to the first end wall.
- Second agitating means provided on the rotating shaft between the means and the second end wall.
- the drying device further includes third stirring means for moving the water-absorbing resin in a rotation direction of the rotating shaft.
- the first stirring means and / or the second stirring means is a ribbon screw.
- the distance between the peripheral end of the first stirring means and the peripheral end of the Z or second stirring means and the peripheral wall is preferably 1 to 20 mm, more preferably 3 to 15 mm.
- the distance between the peripheral end of the first and second stirring means and the peripheral wall may be different. Instead, it is preferable to set the separation distance between the peripheral end of the third stirring means and the peripheral wall in the range.
- FIG. 1 is a process conceptual diagram of a method for producing a water absorbent resin according to the first embodiment of the present invention.
- FIG. 2 is a perspective view of the drying device according to the present invention.
- FIG. 3 is a partially cutaway view of the drying apparatus shown in FIG. 2 along line III-III. In this figure, a part of the peripheral walls of both ends of the drying device is notched.
- FIG. 4 is a partially cutaway view of the drying apparatus shown in FIG. 2 along line IV-IV. In this drawing, both end walls and a part of the peripheral wall of the drying device are notched.
- FIG. 5 is a process conceptual diagram of a water absorbent resin production method according to the second embodiment of the present invention.
- FIG. 6 is a process conceptual diagram of a conventional water absorbent resin production method. BEST MODE FOR CARRYING OUT THE INVENTION
- FIG. 1 is a process conceptual diagram of a method for producing a water absorbent resin according to the first embodiment of the present invention.
- the method for producing a water absorbent resin of the present embodiment includes a polymerization step S1 and a drying step S2.
- a water-absorbent resin is produced in the reaction tank 11 by performing a polymerization reaction by a reversed-phase suspension polymerization method. Specifically, first, an aqueous solution containing a water-soluble ethylenically unsaturated monomer for constituting the resin, a highly hydrophobic solvent that does not significantly dissolve the monomer and the produced polymer, and a monomer aqueous solution for the solvent are prepared. A surfactant for stabilizing dispersion, a radical polymerization initiator and, if necessary, a crosslinking agent are charged into the reaction tank 11 and mixed, and then a radical polymerization reaction is started.
- the reaction tank 11 for example, a so-called batch-type stirring tank that is installed so as to open in the vertical direction can be used.
- the water-soluble ethylenically unsaturated monomer used in the present invention includes, for example, (meth) acrylic acid [“(meth) atari” means “atari” or “metari” And 2- (meth) acrylamide 2-methylpropanesulfonic acid, and alkali metal salts thereof.
- examples of the water-soluble ethylenically unsaturated monomers include nonionic monomers such as (meth) acrylamide, N, N-dimethylacrylamide, 2-hydroxyshethyl (meth) acrylate, and N-methylol (meth) acrylamide.
- unsaturated monomers containing an amino group such as getylaminoethyl (meth) acrylate and tert-aminopropyl (meth) acrylate, and quaternized products thereof.
- acrylic acid, an alkali metal salt thereof, methacrylic acid, an alkali metal salt thereof, acrylamide, methacrylamide, and N, N-dimethylacrylamide can be particularly preferably used.
- One of these monomers may be used, or two or more of them may be used in a single reaction system.
- the concentration of the water-soluble ethylenically unsaturated monomer in the solution of the water-soluble ethylenically unsaturated monomer 7 when charged into the reaction tank 11 is preferably from 25% by weight to a saturated concentration.
- the aqueous monomer solution may be prepared by neutralizing the acid group with an alkali metal.
- the degree of neutralization by the aluminum alloy is determined by ensuring that the resulting water-absorbent resin has a high water absorption rate and avoiding problems with safety due to the presence of excess aluminum metal.
- Alkali metals for neutralization include lithium, sodium, and potassium. In this embodiment, sodium and potassium are particularly preferred.
- the solvent examples include aliphatic hydrocarbons such as n-hexane, n-heptane, and ligroin; alicyclic hydrocarbons such as cyclopentane, methylcyclopentane, cyclohexane, and methylcyclohexane; and , Benzene, toluene, and aromatic hydrocarbons such as xylene.
- aliphatic hydrocarbons such as n-hexane, n-heptane, and ligroin
- alicyclic hydrocarbons such as cyclopentane, methylcyclopentane, cyclohexane, and methylcyclohexane
- Benzene, toluene, and aromatic hydrocarbons such as xylene.
- n-hexane, n-heptane, cyclohexane, toluene, and xylene can be particularly preferably used.
- the amount of the solvent used is preferably 50 to 600 parts by weight, more preferably 100 to 600 parts by weight, based on 100 parts by weight of the water-soluble ethylenically unsaturated monomer. Preferably 100 to 550 parts by weight It is.
- the surfactant examples include nonionic surfactants such as sorbitan fatty acid ester, polyglycerin fatty acid ester, sucrose fatty acid ester, sorbitol fatty acid ester, polyoxetylene alkylphenyl ether, and hexaglyceryl monobehate, And aeon-based surfactants such as fatty acid salts, alkyl benzene sulfonic acid salts, alkyl methyl tartrate salts, polyoxyethylene alkyl phenyl ether sulfate salts, and polyoxyethylene alkyl ether sulfonic acid salts.
- nonionic surfactants such as sorbitan fatty acid ester, polyglycerin fatty acid ester, sucrose fatty acid ester, sorbitol fatty acid ester, polyoxetylene alkylphenyl ether, and hexaglyceryl monobehate
- sorbitan fatty acid ester polyglycerin fatty acid ester, sucrose fatty acid ester, and hexaglyceryl monobelate can be particularly preferably used.
- the amount of the surfactant used is preferably 1 to 5 parts by weight, more preferably 0.2 to 3 parts by weight, per 100 parts by weight of the aqueous solution of the water-soluble ethylenically unsaturated monomer. is there.
- the radical polymerization initiator include water-soluble radical polymerization initiators such as potassium persulfate, ammonium persulfate, and sodium persulfate; and oil-soluble radicals such as peroxydazole benzoyl and azobisisobutyronitrile.
- a redox-based polymerization initiator obtained by using a 7-soluble radical polymerization initiator in combination with a sulfite salt or the like may be employed.
- the amount of the radical polymerization initiator to be used is from 0.05 mmol to 0.05 mol per mol of the water-soluble ethylenically unsaturated monomer from the viewpoint of avoiding a rapid polymerization reaction while shortening the polymerization reaction time. It is preferably 1 mole.
- cross-linking agent examples include, for example, polyethylene glycol, propylene glycol, trimethylolpropane, glycerin, polyoxyethylene glycol, polyoxypropylene glycol, and polyglycerol. Di- or tri (meth) acrylates.
- crosslinking agent examples include unsaturated polyesters obtained by reacting an unsaturated acid such as maleic acid and fumaric acid with polyols, bisacrylamides such as N, N-methylenebisacrylamide, and polyepoxides.
- D) Carpamil di (meth) acrylate obtained by reacting with hydroxyethyl acrylate can also be used.
- compounds having two or more polymerizable unsaturated groups such as arylated starch, arylated cellulose, diallyl phthalate, ⁇ , ⁇ ', ⁇ "-triallyl isocyanate, and dibierbenzene, may be used as the crosslinking agent.
- Diglycidyl ether compounds such as (poly) ethylene glycol diglycidyl ether, (poly) propylene glycol diglycidyl ether, and (poly) glycerin diglycidyl ether, epichronorehydrin, epipromhydrin, and ⁇ -methylepiclor Haloepoxy conjugates such as hydrin, and, in addition, 2,4-tolylene diisocyanate and hexamethylene diisocyanate.
- Dissocyanate compounds having two or more reactive functional groups The amount of the crosslinking agent to be added depends on the amount of the resulting polymer.
- the water-soluble property of the water-absorbent resin is suppressed, and from the viewpoint of obtaining the water-absorbent resin with sufficient water-absorption, the water-soluble ethylenically unsaturated monomer 100 It is preferably 0.001 to 2 parts by weight with respect to parts by weight.
- the aqueous solution of the water-soluble ethylenic unsaturated monomer as described above, a surfactant, a radical polymerization initiator, and a bridge if necessary The reverse phase suspension polymerization is carried out in a water-in-oil system by stirring the agent and the solvent in a solvent while heating. According to the reverse phase suspension polymerization method, the resulting polymer is generally obtained in a granular form. The resulting polymer is obtained with a relatively sharp particle size distribution in correlation with the volume distribution of the aqueous monomer solution as the reaction phase dispersed in the hydrophobic solvent as the non-reaction phase.
- the reaction temperature in the polymerization reaction is appropriately set according to the radical polymerization initiator used.
- the reaction temperature is preferably from 20 to 110 ° C., more preferably from 40 to 80 ° C., from the viewpoint of speeding up the polymerization reaction, shortening the polymerization time, and easily removing the heat of polymerization. ° C.
- the reaction time is preferably 0.5 to 4 hours.
- a so-called seed polymerization method may be employed in order to increase the particle size of the final product particles in the reverse phase suspension polymerization method.
- the seed polymerization method it is preferable to employ a method of growing seed particles by a multi-stage polymerization process.
- the polymerization reaction is carried out in a state where the aqueous solution dissolving the monomer to be dissolved is appropriately dispersed in the solvent, thereby generating primary particles.
- the first-stage polymerization is stopped or terminated, and a significant amount of a surfactant is precipitated and removed from the reaction solution by, for example, cooling, and then a further aqueous monomer solution is added to obtain an appropriate size.
- the agglomerates are grown.
- the second-stage polymerization is performed to crosslink a plurality of primary particles constituting the aggregate to generate 27th-order particles.
- the removal of a significant amount of surfactant before the second stage polymerization reaction is achieved by suppressing the degree of dispersion of the aqueous monomer solution added to perform the second stage polymerization reaction. This is to increase the diameter of the secondary particles used. By going through such a plurality of polymerization steps, the particle diameter of the particles finally obtained in the reversed-phase suspension polymerization method can be appropriately increased.
- the water-absorbing resin produced through the polymerization step S1 is supplied to the next drying step S2 in a slurry state.
- the water absorbent resin is dried by the drying device X1.
- the drying device XI includes end walls 21 and 22, a peripheral wall 23, a rotating shaft 24, and stirring blades 25, 26, and 27. External heating This is configured as a ⁇ -type drying device. Each part is made of, for example, stainless steel. As shown in FIG. 1, a condenser 28 (not shown in FIGS. 2 to 4) is connected to the drying device XI.
- the end walls 21 and 22 and the peripheral wall 23 constitute a substantially cylindrical receiver in the drying device X1.
- a discharge port (not shown) is provided at a predetermined position on the end walls 21 and 22 and the peripheral wall 23 so as to be openable and closable.
- the diameter L1 is 40 Omm and the length L is the inner diameter of the cylindrical receiver formed by the end walls 21 and 22 and the peripheral wall 23. 2 is 420 mm.
- the rotating shaft 24 extends substantially horizontally between the end walls when the device is properly installed, and is connected to a predetermined driving mechanism (not shown). When the device is driven, the rotating shaft portion 24 is rotated by the drive mechanism in a direction indicated by an arrow A in FIGS. In the drying device X 1 of the present embodiment, the diameter L 3 of the rotating shaft portion 24 is 1 65 mm.
- the stirring blades 25, 26, 27 are for stirring the slurry or the water-absorbing resin contained therein.
- the stirring blades 25 and 26 are ribbon screws provided on the rotating shaft portion 24, respectively, and the spiral directions are opposite to each other.
- the surfaces of the stirring blades 25 and 26 facing left in the figure are indicated by hatching.
- each of the stirring blades 27 is a middle blade, and is fixed to the stirring blade 25 or the stirring blade 26.
- the stirring blade 27 may be fixed to the rotating shaft 24.
- the length L4 in the longitudinal direction of the stirring blade 27 is 10 O mm.
- the stirring blade 25 rotates along with the rotating shaft portion 24, and when slurry is charged into the device, moves the slurry existing near itself to the right in the figure. And stir.
- the stirring blade 26 rotates along with the rotating shaft portion 24, and when slurry is charged in the apparatus, moves the slurry existing in the vicinity of itself to the left in the figure. Stir while stirring.
- the stirring blade 27 rotates in accordance with the rotation of the rotating shaft 24, and moves the slurry present near itself in the rotating direction of the rotating shaft 24.
- the configuration of the stirring blades 25, 26, and 27 may be replaced with the configuration of the present embodiment, as long as the stirring operation described above can be achieved for each of them. And so on.
- the distance between the peripheral end of the stirring blade 27 and the peripheral wall 23 is 3 to 15 mm.
- the separation distance sweeps a position farthest from the rotating shaft portion 24 among the stirring blades (stirring blades 25, stirring blades 26, and stirring blades 27) that rotate along with the rotating shaft portion 24. This corresponds to the distance between the edge of the farthest sweeping portion and the peripheral wall 23 in the stirring blade having the portion. Therefore, when the stirring blade 27 is not provided in the drying device XI, it is preferable to set the separation distance between the peripheral end of the stirring blades 25 and 26 and the peripheral wall 23 to 3 to 15 mm.
- the drying step S2 first, the slurry containing the water-absorbing resin generated through the above-described polymerization step S1 is supplied to the drying apparatus X1 having such a configuration through a predetermined inlet (not shown). And put it in.
- the drying device XI is driven, and the slurry is dried while being stirred by the stirring blades 25, 26, and 27 under the temperature and pressure conditions described below. This At this time, the stirring blade 25 stirs the slurry while moving the slurry or the water-absorbing resin contained therein in the right direction in the figure, and the stirring blade 26 moves the slurry or the water absorption contained in the left direction in the figure.
- the slurry is stirred while moving the resin, and the stirring blade 27 moves the slurry or the water-absorbing resin contained in the slurry in the rotation direction of the rotating shaft portion 24.
- Water and solvent in the slurry are distilled off from the slurry and collected in a condenser 28 via a predetermined transfer pipe. The collected water and solvent are discharged from the condenser 28 as appropriate.
- the peripheral end speed of the stirring blade 27 when the apparatus is driven is 0.3 to 0.7 m / s in the present embodiment.
- the peripheral end speed refers to the position of the stirring blade (stirring blade 25, stirring blade 26, and stirring blade 27) farthest from the rotating shaft portion 24 among the stirring blades rotating with the rotating shaft portion 24. This corresponds to the velocity at the edge of the farthest sweeping part in the stirring blade having a portion to be swept. Therefore, when the stirring blade 27 is not provided in the drying apparatus XI, it is preferable to set the peripheral end speed of the stirring blades 25 and 26 to 0.3 to 0.7 m / s.
- the pressure in the drying device X1 in the drying step S2 that is, the pressure in the receiver is set to 20 to 70 kPa, and the temperature is set to 80 to 90 ° C.
- the drying operation performed using the drying apparatus X1 under the above-described conditions is continued until the water content of the water-absorbent resin becomes 10% by weight or less.
- a counterflow is generated near the center of the apparatus mainly due to the rotation of the stirring blades 25 and 26.
- a rotating flow around the rotation axis is generated in the slurry. From the slurry or the water-absorbing resin which is appropriately stirred by such a combination of the counterflow and the rotating flow, a sufficient amount of water can be obtained together with the solvent without causing the resin to clump and unreasonably break. Is removed.
- the water-absorbent resin can be efficiently produced.
- the water content is high. It is possible to remove a sufficient amount of water together with the solvent while preventing the water-absorbent resin from being lumped and unduly crushed.
- FIG. 5 is a process conceptual diagram of a water absorbent resin production method according to the second embodiment of the present invention.
- the method for producing a water absorbent resin according to the present embodiment includes a polymerization step S1, a drying step S2, and a drying step S3.
- a water-absorbent resin is produced in the reaction tank 11 by performing a polymerization reaction by a reversed-phase suspension polymerization method. Specifically, an aqueous solution of a water-soluble ethylenically unsaturated monomer, a surfactant, a radical polymerization initiator, and, if necessary, a cross-linking agent are charged into a reaction vessel 11 and stirred while heating. In this way, reverse-phase suspension polymerization is performed in a water-in-oil system.
- the reaction tank 11, the substances to be used, and the reaction conditions are the same as described above with respect to the first embodiment.
- the water-absorbing resin generated through the polymerization step S1 is supplied to the next drying step S2 in a slurry state.
- the water absorbent resin is dried by the drying device X1.
- the drying device X1 is the same as the above-described drying device X1 in the first embodiment.
- the drying apparatus X1 is turned on.
- the slurry is dried while being driven and stirred by the stirring blades 25, 26, 27.
- water and the solvent in the slurry are distilled off from the slurry and collected in the condenser 28 via a predetermined transfer pipe.
- the peripheral end speed of the stirring blade, and the pressure and temperature inside the device are the same as described above in the first embodiment.
- the drying step S2 of the present embodiment the drying operation is continued until the volume of the slurry reaches the initial 40 to 60%.
- the highly water-absorbent resin obtained by removing most of the water and the solvent in the slurry in the drying step S2 as described above is introduced into the drying device X2.
- the drying device X2 has the same components as the drying device X1, and is designed to be smaller in size than the drying device XI.
- the size of the drying device X 2, particularly the capacity of the receiver, is determined according to the volume of the highly water-absorbent resin obtained through the drying step S 2.
- the water-absorbent resin having a high water content, whose volume has been reduced through the drying step S2 is introduced into the drying apparatus X2, and then the drying apparatus X 2 is driven to dry the water-absorbing
- the water and the solvent in the water-absorbent resin are distilled off from the water-absorbent resin and collected in the condenser 28 via a predetermined transfer pipe.
- the peripheral end speed of the stirring blade, as well as the pressure and temperature inside the device, are the same as those described above with respect to the drying step S2 of the first embodiment.
- the drying operation is continued until the water content of the water absorbent resin becomes 10% by weight or less.
- a plurality of receivers having the configuration shown in FIGS. It is also possible to adopt a three-stage or more drying method in which the drying device is used so that the volume of the receiver is gradually reduced. In this case, the slurry or the water-absorbing resin is transferred to the next drying device after drying to a predetermined volume in each drying device, and the water content of the water-absorbing resin is 10% by weight or less in the last drying device. Continue the drying operation until.
- n-heptane as a solvent is put, and there is a hexylglyceryl monobenelate of HLB 13.1. 1 as a surfactant (trade name: Nonion) GV-106, manufactured by NOF CORPORATION). This was heated to 50 ° C. to dissolve the surfactant, and then cooled to 30 ° C.
- the mixing vessel (2 0 L vol) to prepare a 8 0 weight 0/0 of Akuriru acid solution 3 6 8 0 g, while cooling with ice from the outside of the container, 2 0.1% by weight of water with respect to this by dropwise addition of aqueous sodium solution 6 1 0 4 g oxidized, neutralized 7 5 mole 0/0 of Atariru acid. Thereafter, 4.4 g of potassium persulfate as a polymerization initiator was added thereto and dissolved. Thus, 97788 g of an aqueous acrylic acid solution (first monomer aqueous solution) neutralized with an alkali metal salt was prepared. This first monomer aqueous solution is 20. Keep at C! / Further, 9778 g of the second monomer aqueous solution was prepared in the same manner as in the first monomer aqueous solution, and the sample temperature was maintained at 20 ° C.
- the first monomer 7] solution is poured into the above-mentioned polymerization tank, stirred and dispersed, the system is sufficiently purged with nitrogen, and then heated to perform the first-stage polymerization reaction. Got. At this time, the reaction temperature was 7 ° C., and the reaction time was 3 hours. This first polymerization slurry was cooled to 20 ° C. Next, the second monomer aqueous solution was further poured into the polymerization vessel, stirred and dispersed, and the system was sufficiently purged with nitrogen, and then heated to perform a second-stage polymerization reaction. At this time, the reaction temperature was 70 ° C., and the reaction time was 3 hours.
- the slurry containing the water-absorbent resin produced through the above polymerization step was dried using a stainless steel external heating type drying apparatus having a configuration as shown in FIG.
- This device has stirring blades 25 and 26 which are repone screws and stirring blades 27 which are paddle blades.
- the separation distance between the peripheral end of the stirring blade 27 and the peripheral wall 23 was set to 10 mm.
- the pressure inside the apparatus was 55 kPa
- the temperature was 90 ° C
- the peripheral speed of the stirring blade 27 was 0.3 m / s
- the drying time was 2 hours. 3 hours.
- 620 g of a water-absorbing resin was obtained.
- the water-absorbent resin of this example was manufactured.
- the weight average particle diameter was 450 m
- the content of particles having a particle diameter of 850 m or more was 0.5% by weight or less
- the particle diameter was 106 ⁇ m.
- the content of the following particles was 0.1% by weight or less.
- the content of the residual monomer in the water-absorbent resin of this example was examined.
- 2 g of the water-absorbent resin produced as described above was dispersed in 500 g of a 0.9% by weight food and stirred at room temperature for 1 hour.
- the dispersion solution was filtered to separate the water-absorbent resin from the saline solution.
- the amount of the monomer dissolved in the obtained saline solution was measured using high performance liquid chromatography (HPLC).
- HPLC high performance liquid chromatography
- n-heptane as a solvent
- sorbitan monolaurate of HLB 8.6 as a surfactant (trade name: Noun LP-20R, Nippon Yushi ( 38.8 g was added. This was heated to 50 ° C to dissolve the surfactant, and then cooled to 30 ° C.
- the first monomer aqueous solution is poured into the above-described polymerization tank, stirred and dispersed, and the inside of the system is sufficiently replaced with nitrogen.
- the reaction temperature was 70 ° C., and the reaction time was 3 hours.
- This first polymerization slurry was cooled to 10 ° C.
- the second monomer aqueous solution was further poured into the polymerization vessel, stirred and dispersed, and the system was sufficiently purged with nitrogen, and then heated to perform a second-stage polymerization reaction. At this time, the reaction temperature was 70 ° C., and the reaction time was 3 hours.
- the slurry containing the water-absorbing resin produced through the above-described polymerization step was dried using a stainless steel externally heated horizontal drying apparatus having a configuration as shown in FIG.
- This device has stirring blades 25 and 26 which are repone screws and stirring blades 27 which are paddle blades.
- the separation distance between the peripheral end of the stirring blade 27 and the peripheral wall 23 was set to 5 mm.
- the internal pressure of the apparatus was 65 kPa
- the temperature was 80 ° C
- the peripheral speed of the stirring blade 27 was 0.5 m / s
- the drying time was 1 hour. 8 hours.
- 574 g of a water-absorbent resin was obtained.
- the water-absorbent resin of this example was manufactured.
- the weight average particle size was 340 ⁇ m
- the content of particles having a particle size of 850 m or more was 1.5% by weight or less
- the particle size was 106 ⁇ m.
- the content of particles having a particle size of m or less was 1.0% by weight or less.
- the residual monomer content and the water absorbing ability of the water-absorbent resin of this example were measured in the same manner as in Example 1, and found to be 78 ppm / 69 g /, respectively.
- n-heptane as a solvent Hexaglyceryl monobenelate of HLB 13. 1 as a surfactant (trade name: Nonion GV-106, manufactured by NOF Corporation) 36.8 g
- maleic anhydride male 36.8 g of modified polyethylene to which acid was added (trade name: High Wax 1105A, manufactured by Mitsui Chemicals, Inc.) was added. This was heated to 80 ° C to dissolve the surfactant, and then cooled to 30 ° C.
- the mixing vessel (2 0 L vol) to prepare a 8 0 weight 0/0 of acrylic acid aqueous solution 3 6 8 0 g, while cooling with ice from the outside of the container, 2 0.1% by weight of water with respect to this by dropwise addition of oxidizing Natoriumu water solution 6 1 0 4 g, it was neutralized 7 5 mole 0/0 of Atarinore acid. Thereafter, 4.4 g of potassium persulfate as a polymerization initiator and 736 mg of ethylene glycol diglycidyl ether were added and dissolved therein.
- the first monomer aqueous solution is poured into the above-mentioned polymerization tank, stirred and dispersed, and the system is sufficiently purged with nitrogen, and then heated to perform the first-stage polymerization reaction to obtain a first polymerization slurry.
- the reaction temperature was 70 ° C., and the reaction time was 3 hours.
- This first polymerization slurry was cooled to 20 ° C.
- the second monomer aqueous solution was further poured into the polymerization vessel, stirred and dispersed, and the system was sufficiently purged with nitrogen, and then heated to perform a second-stage polymerization reaction. At this time, the reaction temperature was 70 ° C., and the reaction time was 3 hours.
- the slurry containing the water-absorbing resin produced through the above polymerization step was dried using a stainless steel externally heated horizontal drying apparatus having a configuration as shown in FIG.
- This apparatus has stirring blades 25 and 26 that are response crews and stirring blades 27 that are paddle blades.
- the separation distance between the peripheral end of the stirring blade 27 and the peripheral wall 23 was set to 15 mm.
- the pressure inside the apparatus was set to 65 kPa
- the temperature was set to 80 ° C
- the peripheral speed of the stirring blade 27 was set to 0.3 m / s
- the drying time was set to 2.3 m / s. 0 hours.
- 780 g of a water-absorbent resin was obtained.
- the water-absorbent resin of this example was manufactured.
- the weight average particle diameter was 380 m
- the particles having a particle diameter of 850 ⁇ m or more Content is 1.0 weight. /.
- the content of particles having a particle size of 106 m or less was 0.5% by weight or less.
- the residual monomer content and the water absorption capacity of the water-absorbent resin of this example were measured in the same manner as in Example 1, and found to be 31 ppm and 59 g / g, respectively.
- the water-absorbent resin of this comparative example was produced by performing a polymerization reaction in the same manner as in Example 1 by a two-stage reverse phase suspension polymerization method.
- the resulting slurry containing the water-absorbent resin is transferred to a stainless steel externally heated ⁇ ! Type drying device with stirring blades of a different configuration from the stirring blades 25, 26 and 27 shown in Fig. 2. Dried.
- This apparatus has a disk-type agitating blade to which a blade for stirring the slurry in the rotational direction is attached and which is oriented perpendicular to the rotating shaft. Therefore, in the drying step of this comparative example, the slurry inside the apparatus is not positively or sufficiently moved in the extending direction of the rotary shaft.
- the separation distance between the peripheral end of the stirring blade and the peripheral wall was set to 25 mm.
- the internal pressure of the device was 55 kPa
- the temperature was 90 ° C
- the peripheral speed of the stirring blade was 1.6 m / s
- the drying time was 2.8 hours. did.
- the water absorbent resin of this comparative example was manufactured.
- the weight average particle size was 5100 Aim
- the content of particles having a particle size of 850 / m or more was 16% by weight or less
- the particle size was 1%.
- the content of particles of 0.6 ⁇ m or less is 5.
- the residual monomer content was low, the water-absorbing ability was high, and the particle size distribution was sharp.
- the water-absorbent resin of the comparative example could not obtain a sharp particle size distribution as practicable.
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Health & Medical Sciences (AREA)
- Medicinal Chemistry (AREA)
- Polymers & Plastics (AREA)
- General Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Combustion & Propulsion (AREA)
- Polymerisation Methods In General (AREA)
- Addition Polymer Or Copolymer, Post-Treatments, Or Chemical Modifications (AREA)
Abstract
Description
Claims
Priority Applications (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US10/548,261 US20060168841A1 (en) | 2003-03-06 | 2004-02-26 | Method of manufacturing water absorbing resin and drying apparatus used for the method |
EP04714947A EP1602671A4 (en) | 2003-03-06 | 2004-02-26 | METHOD FOR PRODUCING WATER ABSORBENT RESIN AND DRYING APPARATUS USED THEREFOR |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP2003059418A JP2004269593A (ja) | 2003-03-06 | 2003-03-06 | 吸水性樹脂の製造方法およびこれに用いられる乾燥装置 |
JP2003-059418 | 2003-03-06 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2004078796A1 true WO2004078796A1 (ja) | 2004-09-16 |
Family
ID=32958848
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/JP2004/002328 WO2004078796A1 (ja) | 2003-03-06 | 2004-02-26 | 吸水性樹脂の製造方法およびこれに用いられる乾燥装置 |
Country Status (4)
Country | Link |
---|---|
US (1) | US20060168841A1 (ja) |
EP (1) | EP1602671A4 (ja) |
JP (1) | JP2004269593A (ja) |
WO (1) | WO2004078796A1 (ja) |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN107875940A (zh) * | 2017-12-11 | 2018-04-06 | 江苏光阳动力环保设备有限公司 | 一种混料加热反应器 |
Families Citing this family (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2011144038A (ja) * | 2010-01-18 | 2011-07-28 | Ok Engineering Co Ltd | スクリューコンベア |
WO2017115861A1 (ja) * | 2015-12-28 | 2017-07-06 | 株式会社日本触媒 | 吸水性樹脂の製造方法 |
KR20210139288A (ko) * | 2019-03-08 | 2021-11-22 | 스미토모 세이카 가부시키가이샤 | 흡수성 수지 입자 및 그 제조 방법 |
US11260353B2 (en) | 2019-05-14 | 2022-03-01 | Saudi Arabian Oil Company | Systems and methods for treating viscous media |
EP4094824A4 (en) * | 2021-04-07 | 2024-03-06 | Mizuyoke Co., Ltd. | LIQUID MIXING SCOOP AND MIXING DEVICE |
CN113566530B (zh) * | 2021-08-04 | 2022-03-22 | 安仁县香火堂中药有限公司 | 一种中草药用环保无硫烘干设备 |
Citations (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS62235305A (ja) * | 1986-04-04 | 1987-10-15 | Dai Ichi Kogyo Seiyaku Co Ltd | 高分子量アクリル系重合体の製法 |
JPS6377904A (ja) * | 1986-09-22 | 1988-04-08 | Denki Kagaku Kogyo Kk | 熱可塑性樹脂の製造方法 |
Family Cites Families (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP3763376B2 (ja) * | 1997-12-25 | 2006-04-05 | 株式会社日本触媒 | 親水性樹脂の製造方法 |
-
2003
- 2003-03-06 JP JP2003059418A patent/JP2004269593A/ja active Pending
-
2004
- 2004-02-26 US US10/548,261 patent/US20060168841A1/en not_active Abandoned
- 2004-02-26 EP EP04714947A patent/EP1602671A4/en not_active Withdrawn
- 2004-02-26 WO PCT/JP2004/002328 patent/WO2004078796A1/ja active Application Filing
Patent Citations (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS62235305A (ja) * | 1986-04-04 | 1987-10-15 | Dai Ichi Kogyo Seiyaku Co Ltd | 高分子量アクリル系重合体の製法 |
JPS6377904A (ja) * | 1986-09-22 | 1988-04-08 | Denki Kagaku Kogyo Kk | 熱可塑性樹脂の製造方法 |
Non-Patent Citations (1)
Title |
---|
See also references of EP1602671A4 * |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN107875940A (zh) * | 2017-12-11 | 2018-04-06 | 江苏光阳动力环保设备有限公司 | 一种混料加热反应器 |
CN107875940B (zh) * | 2017-12-11 | 2023-08-15 | 江苏光阳动力环保设备有限公司 | 一种混料加热反应器 |
Also Published As
Publication number | Publication date |
---|---|
JP2004269593A (ja) | 2004-09-30 |
US20060168841A1 (en) | 2006-08-03 |
EP1602671A1 (en) | 2005-12-07 |
EP1602671A4 (en) | 2008-09-17 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
US5124416A (en) | Method for production of absorbent polymer | |
EP2980128B1 (en) | Water-absorbent resin composition production method | |
CN101094695B (zh) | 用于超吸收性聚合物的交联剂 | |
JPH0214361B2 (ja) | ||
JP2008255366A (ja) | 超吸収性重合体の製造のための連続的重合方法 | |
JPH11292919A (ja) | 吸水性樹脂の製造方法 | |
JPH0517509A (ja) | 高吸水性ポリマーの製造法 | |
WO2004083284A1 (ja) | 吸水性樹脂粒子の製造方法 | |
JPH05339381A (ja) | 吸水性樹脂及び吸水剤の製造方法 | |
US8119755B2 (en) | Process for producing water-absorbing polymer particles | |
WO2020067310A1 (ja) | 吸水性樹脂の製造方法 | |
WO2004078796A1 (ja) | 吸水性樹脂の製造方法およびこれに用いられる乾燥装置 | |
JPH01144404A (ja) | 吸水性樹脂の製造方法 | |
JPH08120013A (ja) | 高吸水性樹脂の製造法 | |
WO2005012369A1 (ja) | 吸水性樹脂の製造方法 | |
JPH0931107A (ja) | 吸水性樹脂の製造法 | |
JP2966539B2 (ja) | 含水ゲル状重合体の製造方法 | |
JPH0848721A (ja) | 吸水性樹脂の製造方法 | |
JP5972628B2 (ja) | 熱交換構造体、および該熱交換構造体を備える吸水性樹脂の製造装置 | |
JPH05310806A (ja) | 親水性重合体の製造方法 | |
JP6738979B2 (ja) | 吸水性樹脂製造装置 | |
JP3387717B2 (ja) | 高吸水性樹脂の製造法 | |
JP2003026706A (ja) | 連続凝集装置およびこれを備えた多段重合装置 | |
JP2005247931A (ja) | 吸水性樹脂粒子の製造方法 | |
JP3059236B2 (ja) | 高吸水性ポリマーの造粒法 |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
AK | Designated states |
Kind code of ref document: A1 Designated state(s): AE AG AL AM AT AU AZ BA BB BG BR BW BY BZ CA CH CN CO CR CU CZ DE DK DM DZ EC EE EG ES FI GB GD GE GH GM HR HU ID IL IN IS KE KG KP KR KZ LC LK LR LS LT LU LV MA MD MG MK MN MW MX MZ NA NI NO NZ OM PG PH PL PT RO RU SC SD SE SG SK SL SY TJ TM TN TR TT TZ UA UG US UZ VC VN YU ZA ZM ZW |
|
AL | Designated countries for regional patents |
Kind code of ref document: A1 Designated state(s): BW GH GM KE LS MW MZ SD SL SZ TZ UG ZM ZW AM AZ BY KG KZ MD RU TJ TM AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HU IE IT LU MC NL PT RO SE SI SK TR BF BJ CF CG CI CM GA GN GQ GW ML MR NE SN TD TG |
|
121 | Ep: the epo has been informed by wipo that ep was designated in this application | ||
ENP | Entry into the national phase |
Ref document number: 2006168841 Country of ref document: US Kind code of ref document: A1 |
|
WWE | Wipo information: entry into national phase |
Ref document number: 10548261 Country of ref document: US |
|
WWE | Wipo information: entry into national phase |
Ref document number: 2004714947 Country of ref document: EP |
|
WWP | Wipo information: published in national office |
Ref document number: 2004714947 Country of ref document: EP |
|
WWP | Wipo information: published in national office |
Ref document number: 10548261 Country of ref document: US |