| WO/2011/121358 | COMPOSITE ADDITIVE MATERIALS |
| WO/2002/045855 | METHOD OF STORING AMINOTHIOL-MODIFIED SULFONIC ACID TYPE CATION-EXCHANGE RESIN |
| JP2007530896 | Heat transfer system |
TORSTENFELT BOERJE (SE)
SALOMON HEINZ (SE)
TORSTENFELT BOERJE (SE)
| EP0149783A2 | 1985-07-31 | |||
| EP0143234A1 | 1985-06-05 |
| 1. | Method for treatment and disposal of a spent powdered ionexchange resin, whereby said resin first is suspended, essentially for transportation, and thereafter dewatered, dried and mixed with water and liquid additives, the resulting mixture is disposed into a container (19) where a binder and solid additives are added and mixed, whereafter said mixture of binder, resin and water is left to solidify into a body in which the resin is contained as a filler, characterized in that vapours, which are given off from the resin during treatment, especially vapours given off when said resin is dried and heattreated, are collected in a circuit (17), preferably an ejector circuit, that said vapours■ comprising at least water vapour and volatile organic compounds such as amines are condensed into a condensate, whereby substantially all of said volatile organic compounds are maintained solved in said condensate, that said volatile organic compounds contained solved in the condensate are separated from the condensate, resulting in a condensate substantially free from said volatile organic compounds and a vapour containing said volatile organic compounds, and that said volatile organic compounds are destructed, whereby they are substantially transformed into CO2, H2O and N2, before being released. |
| 2. | Method according to claim 1, characterized in that the condensate which has been freed from substantially all volatile organic compounds is added to the resin and the mixture is filled into a container (19) and together with the solidifying agent, a binder, preferably a hydraulic binder such as a cement, said mixture of resin, solidifying agent and condensate are allowed to solidify. |
| 3. | Method according to claim 1 or claim 2, characterized in that said volatile organic compounds, contained in the vapours separated from the condensate, are oxidized through combustion and/or catalytic oxidation. |
| 4. | Method according to claim 3, characterized in that said oxidized vapours are passed through an absorbent filter (204) or other absorbent media for removal of any organic residues contained in said vapours before said vapours are released. |
| 5. | Method according to any of the preceding claims, characterized in that the solubility of said volatile organic compounds in the condensate is lowered to separate said volatile organic compounds from the condensate. |
| 6. | Method according to claim 5, characterized in that an alkaline agent is added to said condensate to raise the pH of the condensate and reduce the solubility of said organic compounds in the condensate, whereby said volatile organic compounds are separated from said condensate. |
| 7. | Method according to any of the preceding claims, characterized in that said resin if in bead form is, as a pretreatment, crushed, preferably milled, to reduce the particle size of the resin and thus improve the conditions for heattreatment and simultaneously increase the amount of resin that can be added in the solidification matrix without jeopardizing the final product properties. |
| 8. | Plant for treatment and disposal of a spent powdered ion exchange resin, comprising means for suspending (11,13) said resin into a pumpable slurry, preferably in the form of a tank, means for dewatering (15) said resin, preferably in the form of a centrifuge, means for drying (16) said resin, a drier, means for mixing (18) said resin with a binder and water, a mixer, and means for disposing (19) said mixture into a container where said mixture is left to solidify into a body in which the resin is contained as a filler, characterized in that said plant comprises means, in the form of an ejector circuit (17) comprising at least a waterdriven ejector pump (171) , for collecting, condensing and cooling vapours given off from said resin during treatment, especially vapours given off from said resin during drying and heattreatment, said vapours comprising at least water vapour and volatile organic compounds such as methane and amines, means for separating (172) said organic compounds from the condensate, resulting in a condensate substantially free from said volatile organic compounds and a vapour containing said volatile organic compounds, means for destruction (202,203) of said volatile organic compounds, whereby they are substantially transformed into CO2, H2O and 2, before being released. |
| 9. | Plant according to claim 8, characterized in that said ejector circuit (17) comprises suction means (171), preferably in the form of a water driven ejector pump, for collecting vapours given off from the resin during the treatment, cooling means, preferably in the form of water circulating in said ejector circuit and a cooler (173), for condensing the vapours and cooling the condensate and a treatment tank (172) suitable for separation of said volatile organic compounds from said condensate. |
| 10. | Plant according to claim 8 or claim 9, characterized by means for adding an alkaline agent (175) to said condensate, whereby the pH of said condensate is raised so that the solubility of said volatile nitrogen containing organic compounds in the condensate is reduced and said volatile organic compounds and part of the methanol are separated from said condensate. |
| 11. | Plant" according to any of claim 8, claim 9 or claim 10 characterized in that a gas circuit (20) is arranged for treatment of said vapours separated from the condensate, said gas circuit comprising at least means for destruction of said volatile organic compounds contained in said vapours through combustion and/or catalytic oxidation (202,203). |
| 12. | Plant according to claim 11, characterized in that said gas circuit (20) for treatment of said vapours compri ses a combustion unit (203) for destruction of said volatile organic compounds and, downstream of said combustion unit, an absorbent filter (204) , for removal of any organic residues from said vapours. |
| 13. | Plant according to claim 11 and 12, characterized in that said gas circuit (20) for treatment of said vapours can comprise a flame arrester (202) and/or a heat exchanger (201) upstream of the combustion unit for destruction of said volatile organic compounds and, downstream of said combustion unit, a cooler (206) for heat removal before further gas release. |
| 14. | Plant according to any of claims 8 to 13, characterized by a pretreatment unit (24) , preferably in the form of a mill, arranged for reducing the particle size of bead ionexchange resin and thus improve the conditions for heattreating said resin and simultaneously increase the amount of resin that can be added in the solidification matrix without jeopardizing the final product properties. |
TECHNICAL FIELD
The invention relates to a method for treating and disposing of spent ion-exchange resin, whereby the risk of swelling of the solidified resin is reduced and therefore a high resin content is achieved in the solidified waste matrix. The invention is especially applicable to treating radioactive spent ion-exchange resin from nuclear plants. The invention also relates to a device for carrying out said method. The invention particularly collects and treats odorous off-gases that would result in hazardous or otherwise unwanted gas releases inside or outside the plant.
BACKGROUND ART
Waste in the form of spent powdered or bead ion-exchange resins, filter residues or sludges is normally treated and solidified together with a solidifying agent before dis¬ posal. As solidification agents cement, bitumen or organic polymers are normally used.
Prior to solidifying spent ion-exchange resin, it is subjected to a heat-treatment during which the functional groups of the anionic part of said resin is decomposed, resulting in an end product with less tendency to swell when wetted, whereby the risk of swelling of the solidified resin is reduced and therefore a high resin content is achieved in the solidified waste matrix, e.g. > 300 kg dry resin per cement solidified waste matrix. The decomposed functional groups, methanol and amines are released as gases, but will when cooled and transferred to an aqueous phase be absorbed in the water. The amines are in an acidic or neutral aqueous phase present as ions and soluble in the water, but will in an alkaline environment be transferred to a strongly odorous volatile gas. In solidification processes involving an
increase 0 in pH of the mixture (e.g. using cement), a solidi¬ fication of the mixture will result in an undesired release of any volatile organic compounds contained in the mixture. To avoid this it is possible to oxidize the organic com- pounds released during the heat-treatment before further use or discharge, for example using a standard wet oxidation process. However, a wet oxidation process is expensive due to the the need of chemical reagents, the process is diffi¬ cult to bring to 100% organic destruction and it results in large amounts of aqueous residues that may need to be further treated.
One aim of the invention is to provide a method for treat¬ ment of spent ion-exchange resin in such way that not only the treated resin but also the fumes or vapours liberated from the resin during treatment are treated and disposed of in an environmentally sound way.
Another aim of the invention is to provide a plant for carrying out said method for treatment of spent ion-exchange resin.
SUMMARY OF THE INVENTION
The invention relates to a method for treatment and disposal of a spent ion-exchange resin, whereby said resin is sus¬ pended in water to form a pumpable slurry, and after the slurry has been transported into the treatment plant, said resin is de-watered, dried and heat-treated, mixed with water and aqueous additives, the resulting mixture is disposed into a container and mixed with a binder, said mixture of binder, resin and water is left to solidify into a body in which the resin is contained as a filler.
According to the invention vapours which are given off from the resin during treatment, especially vapours given off from said resin during drying and heat-treatment, are collected in a circuit, preferably a water driven ejector
circuit that also functions as a condenser for vapours. Said vapours, which comprise at least water vapour and volatile organic compounds such as amines and alcohols such as methanol, are condensed into a condensate, whereby substantially all of said volatile organic compounds are transferred to non-volatile organic compounds maintained solved in said condensate. Said condensate is thereafter treated in such ' a way that the organic compounds, such as amines contained solved in the condensate are transferred to volatile compounds and separated from the condensate, resulting in a condensate substantially free from said volatile organic compounds and a vapour containing said volatile organic compounds. After separation said volatile organic compounds are destructed, whereby they are substan- tially transformed into CO 2 , H 2 O and 2 , before being released.
In one embodiment of the invention the spent ion-exchange resin is suspended into a pumpable slurry by addition of water to a slurry tank into which the resin is fed. The slurry is pumped to a de-watering unit, preferably in the form of a centrifuge. After de-watering the resin is fed into a dryer, where said resin is dried and heat-treated at approximately 150 °C ± 20 °C under continuous stirring of the resin. Vapours, which are given off from the resin during drying and heat-treatment, are removed from the dryer by a water-driven ejector pump and collected in an ejector- circuit, where the vapours are cooled and condensed by the water circulating within the circuit. Additional cooling is provided by a cooler arranged within the circuit. Said vapour and consequently the condensate obtained comprise volatile organic compounds such as amines which are sepa¬ rated from the condensate through a treatment which pre¬ ferably is administered in a treatment tank arranged adjacent to the ejector circuit. After separation from the condensate said volatile organic compounds are subjected to a destruction treatment which substantially transforms them into Cθ 2 ,H 2 θ and N 2 .
After said volatile organic compounds have been separated from the condensate, said condensate, together with cement property enhancing liquid additives, and if needed extra water, is added to the resin in a mixer. The resulting mixture is filled into a container, e.g. a 200L drum, said container is transferred to a solid additive mixing station where a solidification agent, preferably a hydraulic binder such as a cement, and if needed cement property enhancing solid additives are mixed with the resin-slurry. The resulting mixture of resin, binder and condensate is left in the container and allowed to solidify.
According to one further embodiment of the invention, said volatile organic compounds, after separation from the condensate, are collected as vapours in a gas circuit. The gas circuit is arranged adjacent to the treatment tank and comprising at least means for destruction of said volatile organic compounds through combustion and/or catalytic oxidation. Preferably said gas circuit comprises a combus- tion unit, a moisture separator and, if needed, a flame arrester upstream of the combustion unit and a cooler down¬ stream of the combustion unit. The combustion unit can be a conventional combustion chamber where glowing bodies, such as electrical heating element, spark igniters, burners or any other means are arranged for ignition and combustion of said volatile organic compounds to insignificant amounts (amine reduction >99%) . To avoid leakage of uncombusted organic compounds, an absorbent filter or other form of unit containing absorbent media for removal of any organic residues from vapours can be arranged downstream of the combustion unit. Fluidised beds or sand beds can be arranged as combustion units, especially when the used bed material can be expected to interact with the volatile organic com¬ pounds or the combustion products to reduce the amount of undesired compounds in the flues. Also beds containing a catalyst can be arranged as combustion units, thus reducing the combustion temperature from approximately >800 °C to about 200 to 500 °C . ' Utilised bed material can be expected
to interact with the volatile organic compounds or the com¬ bustion products in a way that significantly (amine reduc¬ tion >99%) will reduce the amount of undesired compounds in the flues.
According to one preferred embodiment of the invention, said separation treatment includes a transformation of said vola¬ tile organic compounds from ionic form in the condensate to gaseous form which causes the volatile organic compounds to evaporate from the condensate. Preferably this formation of gaseous compounds is achieved by addition of an alkaline agent to said condensate in the treatment tank. This addi¬ tion raises the pH of the condensate whereby the ionic form of said organic compounds in the condensate is reduced and the gaseous compounds are formed, so that they evaporate from the condensate. By this procedure an uncontrolled emission and exposure to odorous gaseous organic compounds and waste water needing extra treatment are eliminated.
In case spent bead resin should be treated, it is in many instances advantageous to transform the resin to powdered ion-exchange resin before starting the treatment and thus improve the conditions during treatment and simultaneously reduce the bulk-volume of the resin. Preferably said bead resin is milled in a ball, pebble or rod mill before being added to the slurry tank for suspension and further treat¬ ment in the treatment plant.
BRIEF DESCRIPTION OF THE DRAWING
The appended drawing shows a schematic representation of a plant for carrying out a preferred embodiment of the invention.
DESCRIPTION OF THE PREFERRED EMBODIMENTS
A plant for treatment and disposal of a spent powdered ion- exchange resin is schematically illustrated in figure 1.
Spent powdered ion-exchange resin from intermediate storage drums 10 is emptied into a slurry tank 11 where it is suspended into a pumpable slurry. Said slurry is, through a slurry line 12, fed into a second slurry tank 13. To slurry tank 13 also spent ion-exchange resin directly from operation of the power plant is pumped. Said slurry from slurry tank 13 is fed into the actual treatment plant through a second slurry line 14, either directly to dryer 16 or through mechanical de-watering in a centrifuge 15, preferably a so-called decanter centrifuge. Vapours given off from the resin and/or the slurry during dewatering are collected and fed into a gas circuit 20, while back-water from the decanter 15 is returned to the second slurry tank.
After de-watering the resin is fed into a dryer 16, in the figure illustrated as a conical orbiting screw mixer with a heating jacket 161, heated by a circulating heat transfer fluid that is circulating in said heating jacket 161 and a connected heat transfer circuit 162. During heat-treatment the dryer is kept at a constant pressure slightly below ambient pressure to ensure a substantially complete removal of volatile organic compounds from the resin. An underpres¬ sure in the dryer 16 is achieved by applying a suction from a pump 171, in the form of a water-driven ejector, connected to an ejector circuit 17. Vapours given off during heat- treatment, which at least comprise water-vapour and volatile organic compounds, are collected and condensed in said ejector circuit 17 which apart from the water-driven ejector 171 also comprises at least a treatment tank 172, a cooler 173 and a pump 174. The condensate is dissolved in and cooled by the water circulating in said ejector circuit 17. Further cooling of said circulating water is provided by the cooler 173.
To separate the volatile organic compounds from the conden¬ sate, an alkaline agent is added to the treatment tank 172 by addition means 175. The addition of an alkaline agent raises the pH of the condensate whereby said volatile orga-
nic compounds in the condensate are transformed from ionic to gaseous form so that said volatile organic compounds are driven off from the condensate. Substantially all volatile organic compounds are removed through a gas circuit 20 arranged adjacent to the treatment tank 172. Said vaporised organic compounds which at least comprise amines are sub¬ jected to a destruction treatment, whereby they are trans¬ formed to CO 2 , H 2 O and N 2 . Said gas circuit 20, which in the embodiment shown in the figure collects vapours from the decanter 15 and from the treatment tank 172, comprises a moisture separator/heat exchanger 201, a combustion unit 203 and absorbent unit 204, and could if needed contain a flame arrester 202. The necessary underpressure to prevent leakage to the surroundings is achieved by a fan or blower 205. Oxygen, preferably as air, is added to tank 172 to ensure the removal of the volatile organic compounds from the ejector circuit and to ensure a sufficient but not excessive amount of oxygen for the combustion in combustion unit 203.
The combustion unit 203 can be a conventional combustion chamber where glowing bodies, such as electrical heating elements, spark igniters, burners or any other convenient means are arranged for ignition and combustion of said volatile organic compounds, whereby they are transformed into CO 2 , H 2 O and 2 . To avoid leakage of uncombusted organic compounds, an absorbent unit 204 containing an absorbent filter or a bed of absorbent media is arranged for removal of any organic residues from vapours downstream of the combustion unit. Fluidised beds or sand beds arranged as combustion units 203, especially when used bed material can be expected to interact with the volatile organic compounds or the combustion products to reduce the amount of undesired compounds in the flues, are an optional form of a combustion unit 203.
In other embodiments of the invention said combustion unit 203 is replaced or supplemented by a unit for catalytic
oxidation of volatile organic compounds whereby they are transformed into CO 2 , H 2 O and N 2 .
The heat-treated, dried resin is fed from the dryer 16 into a mixer 18, in the figure illustrated with a conical orbiting screw mixer. To the mixer 18 also water is added. Preferably, the condensate freed from volatile organic compounds is taken from the treatment tank 172 and added to the resin in the mixer 18. Wet additives required for the mixing and/or solidification are prepared in one or more special additives circuits 21 and added to the mixer 18. Cement or any other suitable solidifying agent is added to the resin and water mixture at a separate solid additives station 22 after said mixture of resin and water has been fed into a container 19. Said container 19 is preferably fitted with a built in stirrer 191 and loaded on a transport wagon 192.
In case spent bead resin should be treated, it is in many instances advantageous to transform the resin to powdered ion-exchange resin before starting the treatment and thus improve the conditions during treatment and simultaneously reduce the bulk-volume of the resin. Preferably said bead resin is added to a mill 24, in the form of a ball, pebble or rod mil, before being added to the slurry tank 11,13 for suspension and further treatment in the treatment plant.
Other forms of waste material suitable for the same type of treatment before disposal can also be treated in a plant according to the invention. Waste material free from vola¬ tile compounds likely to evaporate in connection with the solidification can be added directly to the mixer 18. The plant as shown in the figure also comprises connection means 23 for feeding of sludges of such material, for instance evaporator bottoms, into the mixer 18.