JP2009167239A - Apparatus and method for treating ion-exchange resin - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To prevent a reaction vessel or piping from being plugged by a solid material or being corroded when subjecting a used ion-exchange resin to decomposition treatment in the reaction vessel. <P>SOLUTION: An apparatus for treating the ion-exchange resin includes: an oil-forming and separating device 11 for forming oil from the ion-exchange resin with high-temperature high-pressure water, and separating a pretreatment liquid C containing the oil formed from the ion-exchange resin from a remaining solid material D; the reaction vessel 12 for decomposing the pretreatment liquid with the high-temperature high-pressure water; a slurry-transporting line 13 for transporting a slurry A containing the ion-exchange resin to the oil-forming and separating device; a pretreatment liquid-feeding line 14 for feeding the pretreatment liquid from the oil-forming and separating device to the reaction vessel; a first oxidizing agent-feeding line 15 for feeding an oxidizing agent used for forming the oil from the ion-exchange resin to the oil-forming and separating device; a second oxidizing agent-feeding line 16 for feeding an oxidizing agent used for decomposing the pretreatment liquid to the reaction vessel; and a decomposed fluid-transferring line 17 for cooling and pressure-reducing decomposed gas and decomposed liquid formed in the reaction vessel. <P>COPYRIGHT: (C)2009,JPO&INPIT

Description

  The present invention relates to an ion exchange resin processing apparatus and method for decomposing used ion exchange resin.

  In recent years, attention has been paid to a method using high-temperature and high-pressure water (for example, water in a supercritical state) exceeding the critical point of water (temperature: 374.2 ° C., pressure: 22.1 MPa) as a method for treating waste containing organic matter. ing. This method takes advantage of the feature that organic bonds can be broken at high speed because supercritical water (supercritical water) has high energy.

  On the other hand, supercritical water is characterized by a decrease in the solubility of inorganic salts. Therefore, when decomposing used ion exchange resin generated from the condensate purification system of a nuclear power plant in a reaction vessel filled with supercritical water, the ion exchange resin contains sulfur and nitrogen, and is oxidized. Since iron adheres, after decomposition, inorganic substances such as inorganic salts generated from sulfur and nitrogen and iron oxide accumulate on the reaction vessel wall, etc., and the reaction vessel clogs and promotes corrosion. Problems arise.

As a method for solving the problem of depositing inorganic substances, for example, “Solid body separation method and apparatus in wet oxidation type process” (Patent Document 1) is composed of a super zone exceeding the critical temperature and a sub-zone lower than the critical temperature. A substance containing water, organic matter, inorganic matter, and oxygen is supplied into a vertical reaction vessel and reacted in a super zone. Decomposition gas and decomposition solution other than solid matter such as inorganic matter and solid matter deposited at the time of reaction are reversed in the super zone and then discharged out of the reaction vessel through the reaction vessel upper outlet pipe. Solids such as inorganic substances and solids move to the subzone, are dissolved, and are discharged out of the reaction vessel through the reaction vessel lower outlet pipe.
International Publication WO89 / 02874

  However, in the method described in the above-mentioned patent document, when a waste containing a large amount of an inorganic material or a waste material in which a large amount of an inorganic material is deposited after decomposition is treated, the size of a solid material such as an inorganic material and a solid material is small, If the weight is light, solids such as inorganic substances and solids do not move to the subzone, and are accompanied by the flow of cracked gas and cracked liquid. As a result, there is a possibility that the inorganic substance and the solid body move as solid in the reaction vessel upper outlet pipe and block the pipe and the like.

  Thus, when used ion exchange resin is treated in a reaction vessel in high-temperature and high-pressure water containing supercritical water (high-temperature and high-pressure water), the solubility of the inorganic salt decreases, so the walls of the reaction vessel, etc. In addition, solids such as inorganic salts (inorganic substances) and iron oxide (solid bodies) contained in the ion exchange resin are precipitated, and as a result, the reaction vessel and piping may be blocked or corrosion may be accelerated.

  The object of the present invention has been made in consideration of the above-mentioned circumstances, and is an ion that can prevent clogging or corrosion of the reaction vessel or piping by solid matter when decomposing used ion exchange resin in the reaction vessel. An object of the present invention is to provide an apparatus and method for treating exchange resin.

  An apparatus for treating an ion exchange resin according to the present invention is an oil conversion / separation process in which an ion exchange resin is oiled with high-temperature and high-pressure water, and a pretreatment liquid containing oil generated from the ion exchange resin is separated from remaining solids. An apparatus, a reaction vessel for decomposing the pretreatment liquid under high temperature and high pressure water, an ion exchange resin transport line for transporting the ion exchange resin to the oilification / separation apparatus, and a pretreatment liquid from the oilification / separation apparatus A pretreatment liquid supply line for supplying the reaction vessel to the reaction vessel, a first oxidant supply line for supplying an oxidant used for liquefying the ion exchange resin to the oiling / separating device, and a pretreatment liquid are decomposed. And a second oxidant supply line for supplying the oxidant used for the reaction to the reaction vessel, and a decomposed fluid transfer line for cooling and depressurizing the cracked gas and cracked liquid generated in the reaction vessel. It is what.

  Further, in the ion exchange resin processing apparatus method according to the present invention, the ion exchange resin is oiled with high-temperature and high-pressure water in an oil conversion / separation device, and remains with a pretreatment liquid containing oil generated from the ion exchange resin. After the solid is separated, the pretreatment liquid is decomposed in a reaction vessel under high-temperature and high-pressure water.

  According to the apparatus and method for treating an ion exchange resin according to the present invention, when the spent ion exchange resin is decomposed in the reaction vessel, the solid adhered to or contained in the ion exchange resin by the oil converting / separating apparatus. Since the substances are removed in advance, it is possible to prevent the reaction vessel and the pipe connected to the reaction vessel from being blocked or corroded by the solid matter.

  The best mode for carrying out the present invention will be described below with reference to the drawings. However, the present invention is not limited to these embodiments, and the effects of the respective inventions can be obtained by combining the respective embodiments.

[A] First embodiment (FIG. 1)
FIG. 1 is a system diagram showing a first embodiment of the ion exchange resin processing apparatus according to the present invention. The ion exchange resin treatment apparatus 10 shown in FIG. 1 decomposes spent ion exchange resin using high-temperature and high-pressure water (water in a high-temperature and high-pressure state). , A slurry transport line 13 as an ion exchange resin transport line, a pretreatment liquid supply line 14, a first oxidant supply line 15, a second oxidant supply line 16, and a decomposed fluid transfer line 17.

  The slurry transport line 13 transports the slurry A in which water is mixed with the used ion exchange resin to the oil converting / separating device 11. The slurry transport line 13 includes a slurry transporter 19 such as a pump and a valve 20 that are sequentially arranged from the upstream side to the downstream side. During the opening operation of the valve 20, the slurry A is supplied to the oil converting / separating device 11 by driving the slurry transporter 19.

  The oil converting / separating apparatus 11 pulverizes the slurry A containing the used ion exchange resin using high temperature and high pressure water and an oxidizing agent B described later, and includes pretreatment including oil generated from the used ion exchange resin. The liquid C and the solid D are separated. Examples of the solid D include iron oxide attached to or contained in a used ion exchange resin. In order to reliably separate the solid material D, the oil converting / separating device 11 preferably includes a sintered filter or a hollow fiber filter. By these filters, the solid substance D remains in the oil converting / separating apparatus 11.

  Moreover, it is preferable that the oil-formation / separation apparatus 11 is operated at a critical pressure of water of 22.1 Mpa or more. This is because, if the inside of the oil-separating / separating apparatus 11 is equal to or higher than the critical pressure of water, the oiling speed of the used ion-exchange resin is increased, and almost all the used ion-exchange resin is liquefied (liquefied). . Further, the oil converting / separating device 11 is provided with a heater 21 for heating.

  The first oxidant supply line 15 supplies the oxidizer B used for liquefying the used ion exchange resin to the liquefaction / separation apparatus 11. As the oxidizing agent B, oxygen, air, hydrogen peroxide, ozone, or the like is used. In this embodiment, hydrogen peroxide is used.

  The first oxidant supply line 15 includes an oxidant supply unit 22 such as a pump and a valve 23 that are sequentially arranged from the upstream side to the downstream side. During the opening operation of the valve 23, the oxidant B is supplied to the oil conversion / separation device 11 by driving the oxidant supply unit 22.

The oxidizer B supplied from the first oxidizer supply line 15 to the liquefaction / separation apparatus 11 is set to be 1 or more times the amount necessary for liquefying the used ion exchange resin. For example, a cation exchange resin and an anion exchange resin having a dry weight of 1: 1, iron oxide (III) of 1/10 weight of these ion exchange resins, and an oxidant of 0 to 1 with respect to the ion exchange resin, respectively. Double hydrogen peroxide was put in a reaction vessel of about 6 cm ³ and sealed, and an oil formation test was carried out by keeping it at a temperature of 200 ° C. for 2 hours. As a result, the analysis results of the treatment liquid collected from the reaction container after the test were as shown in Table 1 according to the amount of hydrogen peroxide added. That is, by adding an equivalent amount of hydrogen peroxide to the ion exchange resin, it is possible to make all the ion exchange resin oily.

  The pretreatment liquid supply line 14 supplies the reaction container 12 with the pretreatment liquid C that has been separated by the oil purification / separation apparatus 11 and contains the oiled used ion exchange resin. The pretreatment liquid supply line 14 is configured by sequentially arranging a pretreatment liquid transport machine 25 such as a valve 24 and a pump from the upstream side toward the downstream side.

  The second oxidant supply line 16 is for supplying an oxidant used to decompose the pretreatment liquid C to the reaction vessel 12. The second oxidant supply line 16 is branched from between the oxidant supply machine 22 and the valve 23 in the first oxidant supply line 15 and has a valve 26. When the valve 26 is opened, the oxidant B is supplied to the reaction vessel 12 by driving the oxidant supply unit 22. The oxidizing agent led to the reaction vessel 12 is also oxygen, air, hydrogen peroxide, ozone, or the like.

  The reaction vessel 12 decomposes the pretreatment liquid C under the condition of high-temperature and high-pressure water by the action of an oxidant (for example, hydrogen peroxide) supplied from the second oxidant supply line 16 to produce a decomposition gas and a decomposition liquid. (Decomposed fluid E). The reaction vessel 12 is heated by a heater 27.

  The decomposed fluid moving line 17 cools the decomposed fluid (decomposed gas, decomposed liquid) E generated in the reaction vessel 12 and depressurizes it to a normal pressure. The cooler moves from the upstream side to the downstream side. 27 and a pressure reducing valve 29 are sequentially provided.

  Next, the operation of the ion exchange resin processing apparatus 10 configured as described above will be described.

  In the ion exchange resin processing apparatus 10, the used ion exchange resin in the slurry A is liquefied by the action of high-temperature and high-pressure water and the oxidizing agent B in the oil converting / separating apparatus 11, and generated from the used ion exchange resin. The pretreatment liquid C containing the produced oil is separated from the remaining solid substance D such as iron oxide. Thereafter, the pretreatment liquid C is guided to the reaction vessel 12 and decomposed by the action of the high-temperature and high-pressure water and the oxidizing agent B. The operation of the processing apparatus 10 will be specifically described below.

  With the valves 20 and 23 opened and the valves 24 and 26 closed, the slurry transporter 19 and the oxidant supply unit 22 are driven to supply the slurry A and the oxidant B to the oil converting / separating device 11. To do. Next, the slurry transport machine 19 and the oxidizer supply machine 22 are stopped, the valves 20 and 23 are closed, and the oil-separation / separation apparatus 11 is held at 200 ° C. for 2 hours. After 2 hours, the used ion exchange resin is all oiled as shown in Table 1, and the iron oxide adhered to or contained in the ion exchange resin is separated as a solid D.

  Thereafter, the valves 24 and 26 are opened, the oxidant supply unit 22 and the pretreatment liquid transporter 25 are driven, and the pretreatment liquid C in the oiling / separation apparatus 11 is supplied to the reaction vessel 12 and is oxidized. Agent B is supplied to the reaction vessel 12. At this time, the solid substance D remains in the oil converting / separating apparatus 11. In the reaction vessel 12, the pretreatment liquid C containing oil generated from the used ion exchange resin is decomposed by the action of high-temperature and high-pressure water and the oxidizing agent B, and carbon dioxide as decomposition gas and water as decomposition liquid. Is broken down into

  Therefore, according to the said embodiment, there exist the following effects (1)-(3).

  (1) Since the solid matter D such as iron oxide contained or adhered to the used ion exchange resin is separated and removed by the oil-separating / separating device 11, it is oiled by the oil-producing / separating device 11. The reaction vessel 12 for decomposing the pretreatment liquid C containing the used ion exchange resin, the pretreatment liquid supply line 14, the decomposed fluid transfer line 17 and the like can be prevented from being blocked or corroded by the solid substance D. .

  (2) Since the radioactive substance is separated and removed together with the iron oxide adhered to the used ion exchange resin in the oil converting / separating device 11, the pretreatment liquid containing oil generated from the used ion exchange resin The radioactivity level in the reaction vessel 12 for decomposing C is lowered, and measures against the radioactivity applied to the reaction vessel 12 can be relaxed.

  (3) After converting the used ion exchange resin from solid to liquid (oil) in the oil converting / separating apparatus 11, the pretreatment liquid C containing this oil is supplied to the reaction vessel 12 through the pretreatment liquid supply line 14. Therefore, the pretreatment liquid transport machine 25 in the pretreatment liquid supply line 14 is not clogged, and the pretreatment liquid C can be stably supplied to the reaction vessel 12.

[B] Second embodiment (FIG. 1)
In the second embodiment, parts similar to those in the first embodiment are denoted by the same reference numerals, and description thereof is simplified or omitted.

  The ion exchange resin treatment apparatus 30 in the present embodiment is different from the ion exchange resin treatment apparatus 10 in the first embodiment in that the reaction vessel 12 is operated at a critical pressure of water of 22.1 MPa or more. It is the point comprised so that. At this time, the inside of the reaction vessel 12 may be above or below the critical temperature of water (374.2 ° C.) or below, and when it is above 374.2 ° C., the water in the reaction vessel 12 is supercritical. It becomes water.

  Therefore, according to the present embodiment, in addition to the same effects (1) to (3) as in the first embodiment, the following effect (4) is achieved.

  (4) Since the reaction vessel 12 is operated at a pressure equal to or higher than the critical pressure of water, the decomposition rate of the pretreatment liquid C containing oil generated from the used ion exchange resin in the reaction vessel 12 can be increased. . In particular, when the inside of the reaction vessel 12 is at or above the critical pressure and temperature of water, the decomposition rate of the pretreatment liquid C can be further increased by the supercritical water.

[C] Third embodiment (FIG. 2)
FIG. 2 is a system diagram showing a third embodiment of the ion exchange resin processing apparatus according to the present invention. In the third embodiment, the same parts as those in the first embodiment are denoted by the same reference numerals, and the description will be simplified or omitted.

  The ion exchange resin processing apparatus 40 in the present embodiment is different from the ion exchange resin processing apparatuses 10 and 30 of the first and second embodiments in that the reaction container 12 is installed outside and the outer container 42 is installed outside. Thus, a double container structure is formed, and a pressure equalizing maintenance water F pressurized to the same pressure as in the reaction container 12 can be supplied to the gap 43 between the outer container 42 and the reaction container 12. It is a point.

  The pressure equalization maintenance water F is supplied to the gap 43 by a pressure equalization maintenance water supply line 45 provided with a pressure equalization maintenance water supply pump 44. Thereby, the inside of reaction container 12 and the inside of gap part 43 are maintained at the same pressure. Further, the pressure equalization maintenance water F in the gap 43 is discharged to the upstream side of the cooler 28 in the decomposed fluid movement line 17 through the pressure equalization maintenance water discharge line 46, and the decomposition flowing through the decomposed fluid movement line 17. Combined with the finished fluid E.

  In the ion exchange resin processing apparatus 40, the pretreatment liquid C from the oil conversion / separation apparatus 11 is supplied into the reaction container 12 through the pretreatment liquid supply line 14, and the reaction container 12, the outer container 42, The uniform pressure maintenance water F is supplied from the uniform pressure maintenance water supply line 45 to the gap portion 43 between the two. In this state, the pretreatment liquid C is decomposed in the reaction vessel 12 to generate carbon dioxide (decomposed gas) and water (decomposed liquid). The decomposed fluid E (decomposed gas and decomposed liquid) generated by the decomposition of the pretreatment liquid C in the reaction vessel 12 is discharged from the gap 43 while maintaining the pressure equalizing pressure while flowing through the decomposed fluid moving line 17. It joins with the pressure equalization maintenance water F discharged through the line 46, and is cooled and diluted.

  Therefore, according to the present embodiment, in addition to the same effects (1) to (4) as in the first and second embodiments, the following effect (5) is achieved.

  (5) The pressure equalization maintenance water F is supplied from the pressure equalization maintenance water supply line 45 to the gap 43 between the outer container 42 outside the reaction vessel 12 and the reaction vessel 12, and the gap 43 and the reaction vessel 12. Is maintained at the same pressure, the outer container 42 is manufactured from a pressure resistant material, but it is not necessary to manufacture the pressure container 12 from a pressure resistant material, and it is sufficient to manufacture it from a material having a corrosion resistance function. Thus, since the reaction vessel 12 does not need to have both pressure resistance and corrosion resistance, the cost can be reduced.

[D] Fourth embodiment (FIG. 3)
FIG. 3 is a system diagram showing a fourth embodiment of the ion exchange resin treatment apparatus according to the present invention. In the fourth embodiment, the same parts as those in the first embodiment are denoted by the same reference numerals, and the description will be simplified or omitted.

  The ion exchange resin treatment apparatus 50 in the present embodiment is different from the ion exchange resin treatment apparatuses 10 and 30 in the first and second embodiments in that a pretreatment liquid transporter is connected to the pretreatment liquid supply line 14. The water supply line 51 for supplying water G to the oil converting / separating device 11 is connected, and the pretreatment liquid C in the oil converting / separating device 11 is supplied from the water supplying line 51 to the water G Thus, it is configured to be capable of being pumped to the reaction vessel 12 through the pretreatment liquid supply line 14.

  The water supply line 51 for supplying the water G to the oil converting / separating apparatus 11 includes a water supply device 52 such as a pump and a valve 53 on the downstream side of the water supply device 52. When the valve 53 is opened, water G is supplied to the oil making / separation device 11 by driving the water supply device 52, whereby the pretreatment liquid C in the oil making / separation device 11 passes through the pretreatment liquid supply line 14. It is pumped to the reaction vessel 12.

  In this ion exchange resin processing apparatus 50, first, the valves 20 and 23 are opened and the valves 24, 26 and 53 are closed. A and the oxidizing agent B are supplied to the oil converting / separating device 11. Next, the valves 20 and 23 are closed to hold the oil converting / separating device 11 at 200 ° C. for 2 hours. After the elapse of 2 hours, the used ion exchange resin in the slurry A is all liquefied as shown in Table 1 in the oil converting / separating apparatus 11.

  Thereafter, the valves 24, 26 and 53 are opened, and the water supply machine 52 is driven to supply water G to the oil-separation / separation device 11. It is pumped to the reaction vessel 12 through the treatment liquid supply line 14. At the same time, the oxidant B (for example, hydrogen peroxide) is supplied to the reaction vessel 12 through the second oxidant supply line 16 by driving the oxidant supply unit 22. As a result, in the oil making / separating device 11, the solid matter D such as iron oxide adhered to the used ion exchange resin remains in the oil making / separating device 11 and is removed. The oiled used ion exchange resin is decomposed in the reaction vessel 12 to become carbon dioxide (decomposed gas) and water (decomposed liquid).

  Therefore, according to the present embodiment, in addition to the same effects as the effects (1) to (4) of the first and second embodiments, the following effect (6) is achieved.

  (6) The pretreatment liquid C containing the used ion exchange resin that has been liquefied in the liquefaction / separation apparatus 11 is reacted with water G supplied from the water supply line 11 via the pretreatment liquid supply line 14. 12 and the pretreatment liquid transport machine 25 is not installed in the pretreatment liquid supply line 14, so that oil adheres to the pretreatment liquid transport machine 25 and corrodes, or the pretreatment liquid transport machine 25 It is possible to avoid a situation in which malfunction occurs due to inflow.

[E] Fifth embodiment (FIG. 3)
In the fifth embodiment, the same parts as those in the first and fourth embodiments are denoted by the same reference numerals, and the description will be simplified or omitted.

  The difference between the ion exchange resin treatment device 60 in the present embodiment and the ion exchange resin treatment device 50 in the fourth embodiment is that the oilification / separation device 11 is the sulfur in the used ion exchange resin. It is the point comprised so that a part may be removed and ion exchange resin may be oiled after that.

  An experimental result and an effect | action are demonstrated below about the processing apparatus 60 of this ion exchange resin which implements desulfurization and oilification of used ion exchange resin separately as mentioned above.

Cation exchange resin and anion exchange resin having a dry weight of 1: 1, iron (III) oxide of 1/10 weight of these ion exchange resins, and 0 to 1 times as much as each of the ion exchange resins as an oxidizing agent. Hydrogenation test was carried out in which hydrogen peroxide and hydrogen peroxide were put in a reaction vessel of about 6 cm ³ and sealed, and kept at a temperature of 200 to 300 ° C. for 2 hours. As a result, the analysis results of the sample collected from the reaction vessel after the test were as shown in Table 2 according to the amount of hydrogen peroxide added and the temperature. That is, under the condition of no hydrogen peroxide at 300 ° C., the carbon content and sulfur content in the ion exchange resin were transferred to the treatment liquid by 11% and 77%, respectively, and the ion exchange resin remained as a solid. Also, under the condition of hydrogen peroxide 1 time at 200 ° C., the carbon content and sulfur content in the ion exchange resin are transferred to the treatment liquid by 43% and 100%, respectively, and the ion exchange resin does not remain as a solid. The result was that it was oiled.

  In this ion exchange resin processing apparatus 60, first, only the valve 20 is opened, and the valves 23, 24, 26 and 53 are closed, the slurry transporter 19 is driven, and the slurry A is converted into an oil-separating / separating apparatus. 11 is supplied. Next, the valve 20 is closed and the oil-separation / separation apparatus 11 is held at 300 ° C. for 2 hours. After 2 hours, the used ion exchange resin in the oil converting / separating apparatus 11 is not oiled and remains in the oil converting / separating apparatus 11 as a solid, and the sulfur content in the used ion exchange resin is shown in Table 2. As shown in FIG.

  After the elapse of 2 hours, the valves 24, 26, 53 are opened, the water supply device 52 is driven, and the water G supplied from the water supply line 51 increases the sulfur content in the oil-separation / separation device 11. The pretreatment liquid C contained in is fed to the reaction vessel 12 by pressure. Simultaneously with this pumping, the oxidant supply machine 22 is driven to supply the oxidant B to the reaction vessel 12 via the second oxidant supply line 16. Thereby, the sulfur content desulfurized from the used ion exchange resin in the reaction vessel 12 is decomposed.

  After pressure-feeding the pretreatment liquid C containing a large amount of sulfur to the reaction vessel 12, the valve 23 is opened, the valves 24, 26, 53 are closed, and the oxidant B is supplied to the oil making / separating device 11. . Thereafter, the valve 23 is closed, and the oil-separation / separation apparatus 11 is held at 200 ° C. or 300 ° C. for 2 hours. After the elapse of 2 hours, the used ion exchange resin (desulfurized) is all liquefied as shown in Table 2 in the oil converting / separating apparatus 11. At this time, the sulfur content is also decomposed in the reaction vessel 12.

  Thereafter, the valves 24, 26, and 53 are opened, and water G is supplied to the oil making / separating device 11 by driving the water supply device 52, and the pretreatment liquid C in the oil making / separating device 11 is It is pumped to the reaction vessel 12 through the treatment liquid supply line 14. Simultaneously with this pumping, the oxidant B (for example, hydrogen peroxide) is supplied to the reaction vessel 12 through the second oxidant supply line 16 by driving the oxidant supply unit 22. As a result, in the oil making / separating device 11, the solid matter D such as iron oxide adhering to the used ion exchange resin remains in the oil making / separating device 11 and is removed. The used ion exchange resin (desulfurized) is decomposed in the reaction vessel 12 to become carbon dioxide (decomposed gas) and water (decomposed liquid).

  Therefore, according to the present embodiment, in addition to the same effects as the effects (1) to (4) and (6) of the first, second and fourth embodiments, the following effect (7) Play.

  (7) Since the sulfur content in the used ion exchange resin is first removed in the oil converting / separating apparatus 11, the used ion exchange resin is then converted into oil, so that this used oil ion exchange is used. When the resin (desulfurized) is decomposed in the reaction vessel 12, even when the reaction vessel 12 is in a supercritical state, an inorganic salt (for example, ammonium sulfate) generated in the reaction vessel 12 due to the sulfur content is present. Precipitation can be prevented. As a result, the reaction vessel 12 and the decomposed fluid moving line 17 can be reliably prevented from being clogged and corroded by the solid matter such as the inorganic salt or iron oxide.

[F] Sixth embodiment (FIG. 4)
FIG. 4 is a system diagram showing a sixth embodiment of the ion exchange resin treatment apparatus according to the present invention. In the sixth embodiment, the same parts as those in the first and second embodiments are denoted by the same reference numerals, and the description will be simplified or omitted.

  The ion exchange resin processing apparatus 70 in the present embodiment is different from the ion exchange resin processing apparatuses 10 and 30 in the first and second embodiments in that a plurality of the oil converting / separating apparatuses 11 are arranged in parallel. It is installed and each oil-ized / separated apparatus 11 (oil-ized / separated apparatus 11A, 11B, 11C ...) is a point which provided the time difference and was comprised so that oil-ized and a separation process may be implemented.

  That is, the oil conversion / separation process of the used ion exchange resin is finished in one oil conversion / separation device 11 (for example, the oil conversion / separation device 11A), and the generated pretreatment liquid C is decomposed in the reaction vessel 12. During the treatment, the used ion exchange resin is liquefied and separated by another liquefaction / separation device 11 (for example, the liquefaction / separation device 11B).

  Therefore, according to the present embodiment, in addition to the same effects as the effects (1) to (4) of the first and second embodiments, the following effect (8) is achieved.

  (8) Since the liquefaction / separation process in the liquefaction / separation apparatus 11 (the liquefaction / separation apparatuses 11A, 11B, 11C...) And the decomposition process in the reaction vessel 12 can be performed in parallel, The treatment of the exchange resin can be performed efficiently and quickly.

The systematic diagram which shows 1st Embodiment in the processing apparatus of the ion exchange resin which concerns on this invention. The systematic diagram which shows 3rd Embodiment in the processing apparatus of the ion exchange resin which concerns on this invention The systematic diagram which shows 4th Embodiment in the processing apparatus of the ion exchange resin which concerns on this invention. The systematic diagram which shows 6th Embodiment in the processing apparatus of the ion exchange resin which concerns on this invention.

Explanation of symbols

DESCRIPTION OF SYMBOLS 10 Ion exchange resin processing apparatus 11 Oil-ized / separated apparatus 11A, 11B, 11C Oil-ized / separated apparatus 12 Reaction container 13 Slurry transport line (ion-exchange resin transport line)
14 Pretreatment liquid supply line 15 First oxidant supply line 16 Second oxidant supply line 17 Decomposed fluid transfer line 30 Ion exchange resin treatment device 40 Ion exchange resin treatment device 42 Outer container 43 Gap 45 Maintaining pressure equalization Water supply line 50 Ion exchange resin processing device 51 Water supply line 60 Ion exchange resin processing device 70 Ion exchange resin processing device A Slurry B Oxidant C Pretreatment liquid D Solid E Decomposed fluid F Uniform pressure maintaining water G water

Claims (15)

An oiling / separation device that oilizes the ion exchange resin with high-temperature and high-pressure water, and separates the pretreatment liquid containing the oil generated from the ion-exchange resin and the remaining solids,
A reaction vessel for decomposing the pretreatment liquid under high temperature and high pressure water;
An ion exchange resin transport line for transporting the ion exchange resin to the oil-separation / separation device;
A pretreatment liquid supply line for supplying the pretreatment liquid from the oil conversion / separation apparatus to the reaction vessel;
A first oxidant supply line that supplies an oxidizer used to liquefy the ion exchange resin to the liquefaction / separation device;
A second oxidant supply line for supplying an oxidant used for decomposing the pretreatment liquid to the reaction vessel;
An ion exchange resin processing apparatus, comprising: a decomposed fluid moving line for cooling and depressurizing the cracked gas and cracked liquid generated in the reaction vessel. 2. The oxidizer supplied from the first oxidizer supply line to the liquefaction / separation apparatus is set to be 1 or more times the amount necessary for liquefying the ion exchange resin. Ion exchange resin processing equipment. 2. The ion exchange resin processing apparatus according to claim 1, wherein the oil converting / separating apparatus is configured to be operated at a pressure equal to or higher than a critical pressure of water. The ion exchange resin processing apparatus according to claim 1, wherein the reaction vessel is configured to be operated at a pressure equal to or higher than a critical pressure of water. The apparatus for treating an ion exchange resin according to claim 1, wherein the reaction vessel is configured to be operated at a critical pressure of water, a pressure and a temperature higher than the temperature. The reaction container is configured as a double container having an outer container installed outside, and is configured to be able to supply pressure-equalizing maintenance water to a gap between the outer container and the reaction container. The processing apparatus of the ion exchange resin of 1. A water supply line for supplying water is connected to the oil conversion / separation device, and the pretreatment liquid in the oil conversion / separation device is supplied from the water supply line via the pretreatment liquid supply line. 2. The ion exchange resin treatment apparatus according to claim 1, wherein the ion exchange resin treatment apparatus is configured to be capable of being pumped to a reaction vessel. 2. The ion exchange resin according to claim 1, wherein the oil conversion / separation device is configured to first remove sulfur in the ion exchange resin, and then to oil the ion exchange resin. Processing equipment. 2. The ion exchange according to claim 1, wherein a plurality of the liquefaction / separation devices are installed in parallel, and each of the liquefaction / separation devices is configured to perform liquefaction and separation with a time difference. Resin processing equipment. 2. The ion exchange resin processing apparatus according to claim 1, wherein the oil converting / separating apparatus includes a sintered filter or a hollow fiber membrane filter for solids separation. 2. The ion exchange resin treatment apparatus according to claim 1, wherein the oxidant supplied from the first and second oxidant supply lines is at least one member of oxygen, air, hydrogen peroxide, or ozone. . After the ion exchange resin is oiled with high-temperature and high-pressure water in an oil conversion / separation device, the pretreatment liquid containing oil generated from this ion exchange resin and the remaining solid matter are separated,
An apparatus for treating an ion exchange resin, wherein the pretreatment liquid is decomposed in a reaction vessel under high temperature and high pressure water. 13. The ion exchange resin according to claim 12, wherein the pretreatment liquid in the oil conversion / separation apparatus is pumped to a reaction vessel by water supplied to the oil conversion / separation apparatus from a water supply line. Processing method. The oil-exchange / separation apparatus first removes sulfur from the ion-exchange resin, and then the oil-exchange / separation apparatus liquefies the ion-exchange resin. Treatment method of ion exchange resin. The method for treating an ion exchange resin according to claim 12, wherein the high-temperature and high-pressure water in the decomposition treatment is supercritical water.

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