JP2018099690A - Apparatus for recovery of pulp fiber from used sanitary article - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide an apparatus which can recover a pulp fiber and a polymer absorber from a used sanitary article efficiently.SOLUTION: In an apparatus for recovery of a pulp fiber and a polymer absorber from a used sanitary article, the apparatus is configured in a manner that a treatment tank (2) contains an aqueous solution and is loaded with a used sanitary article, water injection means (4-8) inject water to the treatment tank at a first flow rate, aqueous solution discharge means (6,7',8') discharge the aqueous solution from the treatment tank at a second flow rate, and ozone-containing gas introduction means (3,10) treat the used sanitary article while introducing an ozone-containing gas to the aqueous solution, decompose a polymer absorber to lower molecular weight, and solubilize it.SELECTED DRAWING: Figure 1

Description

  The present invention relates to a method for recovering pulp fibers from used sanitary goods. In particular, the present invention relates to a method for recovering pulp fibers from sanitary goods such as used disposable paper diapers containing pulp fibers and polymer absorbents.

  Attempts have been made to recycle used sanitary goods such as disposable disposable diapers. In order to recycle used sanitary goods, usually, used sanitary goods are decomposed in water, separated into components of sanitary goods, and recovered. However, the polymer absorbent material (hereinafter also referred to as “SAP”) contained in sanitary goods absorbs moisture and increases its mass, and also becomes gelled and loses its fluidity. Reduce.

  Therefore, Patent Document 1 has proposed a method of decomposing, solubilizing and removing SAP in used paper diapers by immersing used paper diapers in acidic ozone water having a pH of 3 or less.

JP 2014-217835 A

However, since the method of Patent Document 1 uses acidic ozone water having a pH of 3 or less, it is necessary to add an acid, and it is necessary to treat acidic waste water. Further, depending on the type of acid to be added, oxides are generated by ozone, which may cause a safety problem.
As SAP decomposition progresses, ozone is also consumed in the decomposition of SAP that has been reduced in molecular weight and made water-soluble. As a result, there is a problem that the decomposition efficiency is lowered and it takes time to complete the decomposition.

The present inventors always supply a constant amount of fresh water into the tank during the ozone treatment, and at the same time withdrawing the same amount of treated water, the SAP concentration after decomposition in the treatment tank does not increase, It has been found that SAP can be efficiently decomposed without using water, and the present invention has been completed.
That is, the present invention is a method for recovering pulp fibers from a used sanitary article containing pulp fibers and a polymer absorbent material, the method comprising:
Injecting used sanitary goods into the treatment tank containing the ozone-dissolved aqueous solution, injecting water into the treatment tank at the first flow rate, discharging the aqueous solution from the treatment tank at the second flow rate, and ozone The method includes a step of treating a used sanitary article while decomposing the polymer absorbent material, introducing a gas into the aqueous solution in the treatment tank, decomposing the polymer absorbent material, reducing the molecular weight, and solubilizing.

The present invention includes the following embodiments.
[1] A method for recovering pulp fibers from used sanitary goods including pulp fibers and a polymer absorbent, the method comprising:
The process of putting used sanitary goods into a treatment tank containing an aqueous solution in which ozone is dissolved,
Inject water into the treatment tank at the first flow rate, discharge the aqueous solution from the treatment tank at the second flow rate, and treat used sanitary goods while introducing ozone-containing gas into the aqueous solution in the treatment tank. And a step of decomposing, reducing the molecular weight, and solubilizing the polymer absorbent.
[2] The first flow rate R ₁ (unit: L / min) and the volume V (unit: L) of the aqueous solution in the treatment tank are represented by the formula (1):
0.05 ≦ R ₁ /V≦0.2 (1)
The method according to [1], wherein:
[3] The method according to [1] or [2], wherein the concentration of ozone in the aqueous solution is 1 to 30 ppm by mass.
[4] The method according to any one of [1] to [3], wherein the ozone concentration in the ozone-containing gas is 40 to 60 g / m ³ .
[5] The flow rate R _O (unit: L / min) of the ozone-containing gas and the volume V (unit: L) of the aqueous solution in the treatment tank are expressed by the formula (2):
0.5 ≦ R _O /V≦1.25 (2)
The method according to any one of [1] to [4], wherein:
[6] The product of the concentration (mass ppm) of ozone in the aqueous solution and the time (minutes) of the step of treating the used sanitary goods, decomposing the polymer absorbent, reducing the molecular weight, and solubilizing is 100 to 6000. It is mass ppm * min, The method as described in any one of [1]-[5] characterized by the above-mentioned.
[7] The volume V (unit: L) of the aqueous solution in the treatment tank and the mass W (unit: kg) of the used sanitary product are expressed by the formula (3):
3 ≦ V / W ≦ 50 (3)
The method according to any one of [1] to [6], wherein:
[8] The method according to any one of [1] to [7], further including a step of taking out the residue of the sanitary product from which the polymer absorbent has been removed from the treatment tank.
[9] Further, the residue of the hygiene product from which the polymer absorbent material has been removed is stirred in an aqueous solution containing a disinfectant or in water to clean the residue of the hygiene product and decompose the residue of the hygiene product into components. The method as described in any one of [1]-[8] including the process to do.
[10] The method according to [9], wherein the disinfectant is sodium hypochlorite, chlorine dioxide, acidic electrolyzed water, ozone water, acidic ozone water, or ozone water containing an organic acid.
[11] The method according to [9] or [10], further comprising a step of separating pulp fibers from the residue of the decomposed sanitary goods.
[12] The method according to [11], further comprising a step of washing the separated pulp fiber.
[13] The method according to [12], further comprising a step of dewatering the washed pulp fiber.
[14] The method further includes a step of drying the pulp fiber, and the moisture content of the dried pulp fiber is set to 5 to 13% by the step of drying the pulp fiber. [1] to [13] The method as described in any one of these.
[15] The method according to [14], wherein the pulp fiber is dried at a temperature of 100 to 200 ° C.
[16] The method according to any one of [1] to [15], further including a step of separating and collecting the plastic material.
[17] The method according to any one of [1] to [16], wherein the second flow rate is the same as the first flow rate.
[18] The method according to any one of [1] to [17], wherein the sanitary article is a disposable paper diaper.

  According to the present invention, the polymer absorbent can be efficiently decomposed with ozone without using acidic water, and the pulp fiber can be efficiently recovered from the used sanitary goods including the pulp fiber and the polymer absorbent. be able to.

FIG. 1 is a schematic view of an ozone water treatment apparatus used in the examples. FIG. 2 is a diagram showing the relationship between the treatment time and the wet mass residual rate in the ozone water treatment of Na-SAP. FIG. 3 is a diagram showing the relationship between the treatment time and the wet mass residual rate in the ozone water treatment of U-SAP. FIG. 4 is a graph showing the relationship between the wet mass residual rate and the ozone water concentration in Example 1. FIG. 5 is a graph showing the relationship between the wet mass residual rate and the ozone water concentration in Example 2. FIG. 6 is a diagram showing the relationship between the treatment time and the ozone water concentration in Comparative Examples 1 and 3.

  The present invention is a method for recovering pulp fibers from used sanitary goods comprising pulp fibers and a polymeric absorbent.

The sanitary article is not particularly limited as long as it includes pulp fibers and a polymer absorbent, and examples thereof include disposable paper diapers, urine pads, sanitary napkins, panty liners, and the like.
Used sanitary goods refer to sanitary goods that have absorbed bodily fluids such as manure and menstrual blood.

  Although it does not specifically limit as a pulp fiber, A fluffy pulp fiber, a chemical pulp fiber, etc. can be illustrated.

  A polymer absorbent material is also called a superabsorbent polymer (SAP), which has a three-dimensional network structure in which a water-soluble polymer is appropriately cross-linked and absorbs water several hundred to thousand times. It is insoluble in water, and once absorbed water does not release even when a certain pressure is applied, for example, starch-based, acrylic acid-based, amino acid-based particulate or fibrous polymers can be exemplified. it can.

The method of the present invention comprises:
Injecting used sanitary goods into the treatment tank containing the ozone-dissolved aqueous solution, injecting water into the treatment tank at the first flow rate, discharging the aqueous solution from the treatment tank at the second flow rate, and ozone While introducing the contained gas into the aqueous solution in the treatment tank, it includes a step of treating used sanitary goods, decomposing the polymer absorbent material, reducing the molecular weight, and solubilizing.
The method of the present invention can further be
Removing the sanitary product residue from which the polymer absorbent has been removed from the treatment tank;
A step of washing the sanitary product residue from which the polymer absorbent material has been removed by stirring it in an aqueous solution or water containing a disinfectant to decompose the sanitary product residue into components;
Separating pulp fibers from the residue of decomposed sanitary goods,
Washing the separated pulp fibers,
Dehydrating the washed pulp fiber,
A step of drying the pulp fiber.

The first step is a step of putting used sanitary goods into a treatment tank containing an aqueous solution in which ozone is dissolved (hereinafter, also simply referred to as “feeding step”).
The “aqueous solution in which ozone is dissolved” used in this step is generated, for example, by an ozone generator (ecodesign Ozone Water Exposure Tester ED-OWX-2, Mitsubishi Electric Corporation Ozone Generator OS-25V, etc.). It can prepare by introduce | transducing the ozone-containing gas made into water, and dissolving ozone in water.

  The concentration of ozone in the aqueous solution is not particularly limited as long as it is a concentration capable of decomposing the polymer absorbent, but is preferably 1 to 30 ppm by mass, more preferably 2 to 20 ppm by mass, and Preferably it is 3-10 mass ppm. If the concentration is too low, the polymer absorbent cannot be completely solubilized and the polymer absorbent may remain in the recovered pulp fiber. On the other hand, if the concentration is too high, the oxidizing power is also increased, which may damage the pulp fiber and may cause a problem in safety.

The amount of the aqueous solution in the treatment tank is not particularly limited as long as it is an amount capable of decomposing the polymer absorbent, but the volume V (unit: L) of the aqueous solution in the treatment tank and the mass W of the used sanitary goods. (Unit: kg) is the formula (3):
3 ≦ V / W ≦ 50 (3)
It is preferable to satisfy. More preferably, 5 ≦ V / W ≦ 40, and still more preferably 8 ≦ V / W ≦ 30. If V / W is too small, the polymer absorbent cannot be completely solubilized, and the polymer absorbent may remain in the recovered pulp fiber. On the other hand, if V / W is too large, there is a possibility that the manufacturing cost increases.

The next step is to inject water into the treatment tank at the first flow rate, discharge the aqueous solution from the treatment tank at the second flow rate, and introduce the ozone-containing gas into the aqueous solution in the treatment tank. This is a process of treating finished sanitary goods, decomposing the polymer absorbent, lowering the molecular weight, and solubilizing (hereinafter also simply referred to as “treatment process”).
In this step, the polymer absorbent is decomposed, reduced in molecular weight, and solubilized. Here, the state in which the polymer absorbent is decomposed, reduced in molecular weight, and solubilized refers to a state of passing through a 2 mm screen mesh. That is, in this step, the polymer absorbent is decomposed to such an extent that it passes through a 2 mm screen mesh.
It is preferable to provide a 2 mm screen mesh at the discharge port of the treatment tank. The polymer absorbent decomposed to such an extent that it passes through the 2 mm screen mesh passes through the 2 mm screen mesh and is discharged together with the aqueous solution.

The first flow rate R ₁ (unit: L / min) and the volume V (unit: L) of the aqueous solution in the treatment tank are represented by the formula (1):
0.05 ≦ R ₁ /V≦0.2 (1)
It is preferable to satisfy. More preferably, 0.05 ≦ R ₁ /V≦0.15, and still more preferably 0.075 ≦ R ₁ /V≦0.10. If R ₁ / V is too small, the COD concentration in the treated water increases and the polymer absorbent cannot be completely solubilized. If R ₁ / V is too large, the time for ozone to dissolve in water is short. Therefore, it is difficult to maintain a high ozone concentration, and the polymer absorbent cannot be completely solubilized.

  The first flow rate (hereinafter also referred to as “injection flow rate”) and the second flow rate (hereinafter also referred to as “discharge flow rate”) are preferably the same. By making the first flow rate and the second flow rate the same, the amount of the aqueous solution in the treatment tank can be kept constant. If the amount of the aqueous solution in the treatment tank can be kept substantially constant, that is, if the amount of the aqueous solution in the treatment tank is not significantly increased or decreased, the first flow rate and the second flow rate change over time. May be. The first flow rate and the second flow rate do not always have to be completely the same, but may be approximately the same on average over time. Here, “substantially the same” means that the difference is within 5%.

The treatment step is performed while introducing the ozone-containing gas into the aqueous solution in the treatment tank.
The concentration of ozone of the ozone-containing gas is preferably 40 to 60 g / ^{m 3,} more preferably from 40 to 50 g / ^{m 3,} more preferably from 42.5~45g / ^{m 3.} If the concentration is too low, the polymer absorbent cannot be completely solubilized, and if the concentration is too high, damage to the pulp fibers, a decrease in safety, and an increase in production costs may occur.

The flow rate R _O (unit: L / min) of the ozone-containing gas and the volume V (unit: L) of the aqueous solution in the treatment tank are expressed by the formula (2):
0.5 ≦ R _O /V≦1.25 (2)
It is preferable to satisfy. More preferably, 0.5 ≦ R _O /V≦1.0, and still more preferably 0.5 ≦ R _O /V≦0.75. If R _O / V is too small, the polymer absorbent cannot be completely solubilized, and if R _O / V is too large, it may lead to damage of pulp fibers, reduced safety, and increased manufacturing costs. .

The time for the treatment step is not particularly limited as long as the time can decompose the polymer absorbent material. The time for the treatment step may be short if the ozone concentration of the aqueous solution is high, and it takes a long time if the ozone concentration of the aqueous solution is low.
The product of the concentration (mass ppm) of ozone in the aqueous solution and the time (minute) of the treatment step (hereinafter also referred to as “CT value”) is preferably 100 to 6000 ppm · min, more preferably 200 to 4800 ppm · min. More preferably, it is 300 to 3600 ppm · min. If the CT value is too small, the polymer absorbent cannot be completely solubilized and the polymer absorbent may remain in the recovered pulp fiber. On the other hand, if the CT value is too large, it may lead to damage of pulp fibers, a decrease in safety, and an increase in manufacturing costs.

  In the treatment step, the contents of the treatment tank may be stirred during the treatment, but may not be stirred. Moreover, you may generate | occur | produce a weak flow in aqueous solution by the raise of the bubble of ozone containing gas. The temperature of the aqueous solution is not particularly limited as long as it can decompose the polymer absorbent material. The aqueous solution may be heated, but may remain at room temperature.

  In the treatment process, the polymer water-absorbing material is subjected to an oxidative decomposition action by ozone, the three-dimensional network structure of the polymer water-absorbing material is broken, and the polymer water-absorbing material loses water retention, has a low molecular weight, and is solubilized. The polymer water-absorbing material having increased fluidity dissolves in the aqueous solution. The decomposed polymer absorbent dissolved in the aqueous solution is discharged together with the aqueous solution, and no solid particles of the polymer absorbent remain in the residue of used sanitary goods. In addition, hot melt adhesives used for joining sanitary goods are also oxidized and deteriorated by ozone, and the joining strength between components of the sanitary goods is weakened. Furthermore, in this process, used sanitary goods are primarily sterilized by the sterilizing action of ozone.

  The method of the present invention can further include a step of removing the residue of the sanitary product from which the polymer absorbent material has been removed from the treatment tank (hereinafter also simply referred to as “removal step”). The method for taking out the sanitary product residue from the treatment tank is not particularly limited. For example, the sanitary product residue in the aqueous solution is scooped with a mesh having an opening of 2 mm. Conversely, after discharging the aqueous solution from the treatment tank through a 2 mm screen mesh, the sanitary product residue may be removed from the treatment tank.

  In the method of the present invention, the residue of the sanitary product from which the polymer absorbent has been removed is agitated in an aqueous solution or water containing a disinfectant, thereby cleaning the sanitary product residue and using the sanitary product residue as a component. A step of decomposing (hereinafter simply referred to as “cleaning / decomposing step”) may be further included.

The water used in the cleaning / decomposition process does not necessarily include a disinfectant, but an aqueous solution containing the disinfectant may be used. The disinfectant is not particularly limited, and examples thereof include sodium hypochlorite, chlorine dioxide, acidic electrolyzed water, ozone water, acidic ozone water, and ozone water containing organic acids. From the viewpoint of properties, sodium hypochlorite is preferred.
When an aqueous solution containing a disinfectant is used, the concentration of the disinfectant in the aqueous solution containing the disinfectant is not particularly limited as long as the disinfecting effect is exhibited, but is preferably 10 to 300 ppm by mass, more preferably It is 30-280 mass ppm, More preferably, it is 50-250 mass ppm. If the concentration is too low, a sufficient disinfection effect cannot be obtained, and bacteria or the like may remain in the recovered pulp fiber. On the other hand, if the concentration is too high, not only will the disinfectant be wasted, but the pulp fibers may be damaged and safety problems may occur.

  The stirring in the washing / decomposing step is not particularly limited as long as the sanitary product residue is washed and decomposed into components, and can be performed using, for example, a washing machine. The conditions for stirring are not particularly limited as long as the residue of the sanitary product is washed and decomposed into components. For example, the stirring time is preferably 5 to 60 minutes, more preferably 10 to 50 minutes, More preferably, it is 20 to 40 minutes.

  In the cleaning / decomposing process, the residue of the sanitary product from which the polymer absorbent material has been removed is cleaned, and the sanitary product is broken down into components. In the above treatment process, the hot melt adhesive used for the joining of sanitary goods is oxidized and deteriorated by ozone, and the joining strength between the sanitary goods components is weakened. The hygiene product can be easily broken down into components by stirring. When an aqueous solution containing a disinfectant is used, disinfection with a disinfectant is also performed.

After the washing / decomposing step, a step of separating pulp fibers from the residue of the decomposed sanitary goods (hereinafter simply referred to as “pulp fiber separating step”) can be provided.
The method for separating the pulp fibers from the decomposed sanitary product residue is not limited, and can be performed, for example, by scooping the pulp fibers floating in the liquid containing the decomposed sanitary product residue. .

After the pulp fiber separation step, a step of washing the separated pulp fibers (hereinafter referred to as “pulp fiber washing step”) can be provided.
The method for washing the separated pulp fibers is not limited, but for example, the separated pulp fibers can be put in a mesh bag and rinsed with water. Rinsing may be performed in a batch system, a semi-batch system, or a flow system. When performing by a batch type, it can rinse, for example using a washing machine.
The washing conditions are not particularly limited as long as substances other than pulp fibers are sufficiently removed. For example, the washing time is preferably 3 to 60 minutes, more preferably 5 to 50 minutes, and further preferably. Is 10 to 40 minutes. When performing by a batch type, the amount of water to be used is preferably 500 to 5000 parts by mass, more preferably 800 to 4000 parts by mass, and still more preferably 100 parts by mass (absolutely dry mass) of pulp fibers. 1000 to 3000 parts by mass.

After the pulp fiber washing step, a step of dewatering the washed pulp fiber (hereinafter referred to as “pulp fiber dehydration step”) can be provided.
The method for dewatering the washed pulp fibers is not limited. For example, the washed pulp fibers contained in the mesh bag can be dehydrated with a dehydrator.
The dehydration conditions are not particularly limited as long as the moisture content can be lowered to the target value. For example, the dehydration time is preferably 1 to 10 minutes, more preferably 2 to 8 minutes, Preferably it is 3 to 6 minutes.

  The pulp fiber washing step and the pulp fiber dehydration step may be performed once, but may be alternately repeated a plurality of times.

The method of the present invention can further include a step of drying pulp fibers (hereinafter referred to as “pulp fiber drying step”).
The pulp fiber drying step is performed after at least the pulp fiber separation step. Preferably, it is performed after the pulp fiber washing step or the pulp fiber dehydration step.
Although the method of drying a pulp fiber is not limited, For example, it can carry out using dryers, such as a hot air dryer.
The drying conditions are not particularly limited as long as the pulp fibers are sufficiently dried. For example, the drying temperature is preferably 100 to 200 ° C, more preferably 110 to 180 ° C, and still more preferably 120 to 200 ° C. 160 ° C. The drying time is preferably 10 to 120 minutes, more preferably 20 to 80 minutes, and further preferably 30 to 60 minutes.
The moisture content of the pulp fiber after drying is preferably 5 to 13%, more preferably 6 to 12%, and further preferably 7 to 11%. If the moisture content is too low, hydrogen bonds may become strong and become too hard. Conversely, if the moisture content is too high, mold or the like may occur.

The moisture content of the pulp fiber is measured as follows. This measurement is performed in an atmosphere of 20 ° C. ± 1 ° C.
(1) The mass A (g) of a container (container without a lid) into which a sample to be measured is placed is measured.
(2) About 5 g of a sample to be measured is prepared, placed in the container whose mass was measured in (1), and the mass B (g) of the container containing the sample is measured.
(3) The container containing the sample is placed in an oven set to a temperature of 105 ° C. ± 3 ° C. for 2 hours.
(4) Remove the container containing the sample from the oven and place it in a desiccator (drying agent: one containing colored silica gel) for 30 minutes.
(5) Remove the container containing the sample from the desiccator and measure the mass C (g).
(6) The moisture content (%) is calculated by the following formula.
Moisture content (%) = (B−C) / (C−A) × 100

  The method of the present invention may further include a step of separating and collecting the plastic material (hereinafter referred to as “plastic material separating and collecting step”). Here, a plastic material means a nonwoven fabric material, a film material, an elastomer material, etc. The plastic material separation / recovery step can be performed in parallel with the pulp fiber separation step after the washing / decomposition step. The plastic material separation / recovery step can include a washing step, a dehydration step and a drying step similar to the pulp fiber washing step, the pulp fiber dehydration step and the pulp fiber drying step. The recovered plastic material can be used as a solid fuel by, for example, RPF processing.

  In batch (batch) treatment, the high molecular weight water-absorbing material (SAP) decomposes and becomes water-soluble by lowering the molecular weight, and countless low-molecular weight substances dissolve in the aqueous solution. Ozone is consumed in large quantities in the decomposition of substances, and it is difficult to increase the decomposition efficiency. On the other hand, by constantly replacing a certain amount of aqueous solution with water, the concentration of low-molecular weight SAP that has become water-soluble decreases, and ozone is mainly high. Since it can be consumed for the decomposition of the molecular weight SAP, the decomposition efficiency can be increased. Accordingly, SAP can be efficiently decomposed and removed without treatment in acid (organic acid) water such as citric acid.

  Since the method of the present invention reduces the molecular weight by decomposing the polymer water-absorbing material with ozone and solubilizes it, the polymer water-absorbing material can be dissolved in the aqueous solution and discharged together with the aqueous solution. The polymer water-absorbing material does not remain between the pulp fibers, and the ash pulp fibers that meet the sanitary material standards can be efficiently recovered. According to the method of the present invention, since a metal salt such as lime is not used to deactivate the water absorption capacity of the polymer water-absorbing material, ash derived from the deactivated polymer water-absorbing material (Ca cross-linked body) is not detected. Further, according to the method of the present invention, the polymer water-absorbing material is solubilized, so that the fluidity in the treatment tank is not lost by the swollen polymer water-absorbing material, and the capacity of the processing apparatus is not lowered. Moreover, according to the method of the present invention, the polymer absorbent can be decomposed and solubilized at a relatively low concentration of dissolved ozone concentration of 1 to 30 ppm, and can be processed safely. Further, according to the method of the present invention, in the ozone water immersion process, the hot melt adhesive used for joining sanitary goods is oxidized and deteriorated with ozone water, and the joining strength between the components of the sanitary goods becomes weak. Therefore, in the cleaning / decomposition process, the sanitary product can be easily decomposed into components by stirring.

  Further, according to the method of the present invention, in the first stage, the recovered diaper is immersed in an aqueous solution in which ozone is dissolved, and the polymer absorbent is oxidatively decomposed by the oxidizing power of ozone. In the next cleaning process, dirt and additional disinfection (secondary disinfection) that cannot be removed with ozone water are performed, and then separated into pulp fibers and other materials (plastic materials, etc.). Each is then heated and dried, followed by drying and heat disinfection (tertiary disinfection). By dissolving and removing the polymer absorbent at the initial stage, it can be efficiently recycled with a simple process, and by using ozone water to dissolve the polymer absorbent, a total of three disinfections can be achieved. It is possible to ensure a level of safety.

[Preparation of polymer absorbent sample]
1.5 g of a polymer absorbent (Sumitomo Seika Co., Ltd. super absorbent polymer “Aquakeep” SA60) was put in a bag made of PE mesh sheet (PE200, Samplertech, opening 102 μm). It was impregnated with 80 mL of 0.9% physiological saline for 15 minutes and subjected to water absorption treatment. Thereafter, the bag was pulled up, allowed to stand on a draining net for 15 minutes, drained, and wet weight measurement was performed. This absorbed polymer absorbent was defined as Na-SAP.
1.5 g of a polymer absorbent (Sumitomo Seika Co., Ltd. super absorbent polymer “Aquakeep” SA60) was put in a bag made of PE mesh sheet (PE200, Samplertech, opening 102 μm). It was impregnated with 80 mL of artificial urine for 15 minutes to perform water absorption treatment. Thereafter, the bag was pulled up, allowed to stand on a draining net for 15 minutes, drained, and wet weight measurement was performed. Artificial urine was prepared by dissolving 20 g of urea, 8 g of sodium chloride, 0.8 g of magnesium sulfate heptahydrate, and 0.3 g of calcium chloride dihydrate in 1000 mL of distilled water. This absorbed polymer absorbent was defined as U-SAP.

[Ozone water treatment equipment]
The apparatus used for the ozone water treatment is shown in FIG. The ozone water treatment apparatus 1 includes a treatment tank 2 made of a 2 L glass container, an ozone generator 3, and a water tank 4. A water injection pipe 5 and a water discharge pipe 6 are attached to the treatment tank 2. The water tank 4 and the processing tank 2 are connected by a water injection pipe 5, and a tubing pump 7 and a two-way cock 8 are installed in the water injection pipe 5. The water discharge pipe 6 is also provided with a two-way cock 8 'and a tubing pump 7'. The ozone-containing gas 9 generated by the ozone generator 3 is supplied to the treatment tank 2 through the gas introduction pipe 10. 11 is a gas discharge pipe, 12 is an aqueous solution in which ozone is dissolved (hereinafter also referred to as “ozone water”), and 13 is a polymer absorbent material sample. As the ozone generator 3, an ozone water exposure tester ED-OWX-2 manufactured by Ecodesign Co., Ltd. was used.

[Wet mass remaining rate]
The wet mass residual ratio of the polymer absorbent material sample was calculated by the following formula.
Wet mass residual rate (%) = W / W ₀ × 100
W: Wet mass of the polymer absorbent material sample after treatment W ₀ : Wet mass of the polymer absorbent material sample before treatment

[Measurement of ozone concentration in aqueous solution]
85 mL of an aqueous solution in which ozone was dissolved was placed in a 100 mL graduated cylinder containing about 0.15 g of potassium iodide and 5 mL of 10% citric acid solution. After the reaction, it was transferred to a 200 mL Erlenmeyer flask. A starch solution was added thereto and colored purple, followed by titration with stirring until 0.01 mol / L sodium thiosulfate became colorless.
The concentration of ozone in the aqueous solution was calculated from the titration value using the following formula.
Concentration of ozone in aqueous solution (mass ppm) = 0.01 mol / L sodium thiosulfate (mL) × 0.24 × 0.85 (mL) required for titration

Example 1
2 L of ozone water 12 having an ozone concentration of about 5 ppm was prepared in the treatment tank 2 using the ozone generator 3. Na-SAP as the prepared polymer absorbent material sample 13 was immersed in the ozone water 12 in the treatment tank 2 for 5 minutes. After 5 minutes, the tubing pumps 7 and 7 'are operated, and water injection is started at a flow rate of 0.2 to 0.3 L / min. At the same time, the waste water in the glass container is discharged at a flow rate of 0.2 to 0.3 L / min. I started. During the treatment, ozone-containing gas 9 having an ozone gas concentration of about 40 g / m ³ was continuously supplied from the ozone generator 3 at a flow rate of 1.0 L / min, and ozone water was continuously generated in the treatment tank 2. The treatment was performed after drying the treated polymer absorbent sample at 105 ° C. for 12 hours until the measured dry mass was very small and measurement was difficult. After the treatment, a wet mass measurement of the polymer absorbent material sample 13 was performed. The relationship between the treatment time and the wet mass residual rate is shown in FIG. The relationship between the wet mass residual rate and the ozone water concentration is shown in FIG.

Comparative Example 1
The same operation as in Example 1 was performed except that the processing was performed without operating the tubing pumps 7 and 7 '. The relationship between the treatment time and the wet mass residual rate is shown in FIG. The relationship between processing time and ozone water concentration is shown in FIG.

Comparative Example 2
The same procedure as in Comparative Example 1 was performed except that citric acid was dissolved in ozone water at a concentration of 1% by mass. The relationship between the treatment time and the wet mass residual rate is shown in FIG.

Example 2
It implemented like Example 1 except having changed Na-SAP into U-SAP. The relationship between the treatment time and the wet mass residual rate is shown in FIG. The relationship between the wet mass residual rate and the ozone water concentration is shown in FIG.

Comparative Example 3
The same operation as in Example 2 was performed except that the processing was performed without operating the tubing pumps 7 and 7 '. The relationship between the treatment time and the wet mass residual rate is shown in FIG. The relationship between processing time and ozone water concentration is shown in FIG.

Comparative Example 4
The same procedure as in Comparative Example 3 was performed except that citric acid was dissolved in ozone water at a concentration of 1% by mass. The relationship between the treatment time and the wet mass residual rate is shown in FIG.

As for the ozone water treatment of Na-SAP, as shown in FIG. 2, in Example 1, the treatment of the polymer absorbent material sample could be completed in a short time of 2 hours. That is, it means that the polymer absorbent material sample was decomposed in 2 hours. From this, it can be seen that the polymer absorbent can be decomposed more efficiently by carrying out the flow method than in the batch method (batch method).
As for the ozone water treatment of U-SAP, as shown in FIG. 3, in Example 2, the treatment of the polymer absorbent material sample could be completed in a short time of 3 hours. That is, it means that the polymer absorbent material sample was decomposed in 3 hours. From this, it is understood that the polymer absorbent material can be decomposed more efficiently by performing the flow method than in the batch method.

  As for the relationship between the ozone water concentration and the wet weight residual rate, in the case of the batch type, the ozone water concentration is remarkably reduced (down to 0 ppm) as the wet weight residual rate decreases (see FIG. 6). As shown in FIGS. 4 and 5, in the method of the present invention, it was possible to maintain a high ozone water concentration as compared with the batch method. From this, it is considered that high decomposition efficiency could be obtained compared with the batch type.

  The pulp fiber recovered by the method of the present invention can be suitably used again for the production of sanitary goods.

DESCRIPTION OF SYMBOLS 1 Ozone water treatment apparatus 2 Treatment tank 3 Ozone generator 4 Water tank 5 Water injection pipe 6 Water discharge pipe 6
7, 7 'Tubing pump 8, 8' Two-way cock 9 Ozone-containing gas 10 Gas introduction pipe 11 Gas discharge pipe 12 Ozone-dissolved aqueous solution 13 Polymer absorbent material sample

Claims (18)

An apparatus for recovering pulp fibers from a used sanitary article comprising pulp fibers and a polymeric absorbent, the apparatus comprising:
A treatment tank for storing an aqueous solution in which ozone is dissolved;
Water injection means for injecting water into the treatment tank;
An aqueous solution discharging means for discharging the aqueous solution from the treatment tank;
Ozone-containing gas introduction means for introducing ozone-containing gas into the aqueous solution in the treatment tank;
With
The treatment tank is filled with used sanitary goods in the aqueous solution, the water injection means injects the water into the treatment tank at the first flow rate, and the aqueous solution discharge means is supplied from the treatment tank While discharging the aqueous solution at a second flow rate, the ozone-containing gas introduction means treats used sanitary goods while introducing the ozone-containing gas into the aqueous solution, and decomposes the polymer absorbent, Configured to lower molecular weight and solubilize,
apparatus. The first flow rate R ₁ (unit: L / min) and the volume V (unit: L) of the aqueous solution in the treatment tank are represented by the formula (1):
0.05 ≦ R ₁ /V≦0.2 (1)
Meet,
The apparatus of claim 1. The concentration of ozone in the aqueous solution is 1 to 30 ppm by mass.
The apparatus according to claim 1 or 2. The apparatus of any one of Claims 1-3 whose density | concentration of the ozone in the said ozone containing gas is 40-60 g / m < ³ >. The flow rate R _O (unit: L / min) of the ozone-containing gas and the volume V (unit: L) of the aqueous solution in the treatment tank are represented by the formula (2):
0.5 ≦ R _O /V≦1.25 (2)
Meet,
The apparatus of any one of Claims 1-4.   The product of the concentration (mass ppm) of ozone in the aqueous solution and the used sanitary goods, the polymer absorbent is decomposed, the molecular weight is reduced, and the time (minutes) for solubilization is 100 to 6000 mass ppm. The device according to any one of claims 1 to 5, which is a minute. The volume V (unit: L) of the aqueous solution in the treatment tank and the mass W (unit: kg) of the used sanitary ware are expressed by the formula (3):
3 ≦ V / W ≦ 50 (3)
Meet,
The apparatus according to claim 1. The treatment tank includes a screen at a discharge port of the aqueous solution,
The water injection means stops injection of the water, the ozone-containing gas introduction means stops introduction of the ozone-containing gas, and the aqueous solution discharge means is removed from the treatment tank via the discharge port provided with the screen. The aqueous solution is discharged, and the residue of the used sanitary product from which the polymer absorbent material has been removed is configured to remain in the treatment tank.
The device according to claim 1. Washing and decomposing means for cleaning the residue and decomposing the residue into components by stirring the residue in an aqueous solution containing a disinfectant or in water,
The apparatus according to claim 8. The disinfectant is sodium hypochlorite, chlorine dioxide, acidic electrolyzed water, ozone water, acidic ozone water, or ozone water containing an organic acid.
The apparatus according to claim 9. Further comprising separation means for separating pulp fibers from the decomposed residue.
The apparatus according to claim 9 or 10. A cleaning means for cleaning the separated pulp fiber;
The apparatus of claim 11. Further comprising a dehydrating means for dewatering the washed pulp fiber.
The apparatus according to claim 12. A drying means for drying the dehydrated pulp fiber;
It was comprised so that the moisture content of the said pulp fiber after drying might be 5-13%,
The apparatus of claim 13. The temperature for drying the pulp fiber is 100 to 200 ° C.
The apparatus according to claim 14. The apparatus further comprises a separation and recovery means for separating and collecting the plastic material from the decomposed residue.
Device according to any one of claims 9 or 10. The second flow rate is the same as the first flow rate;
The apparatus according to claim 1. The used sanitary ware is a used disposable paper diaper,
The apparatus according to claim 1.

Images