EP0243557A1 - Apparatus and method for removing strontium and/or cesium ions from an aqueous solution containing chemical hardness - Google Patents

Apparatus and method for removing strontium and/or cesium ions from an aqueous solution containing chemical hardness Download PDF

Info

Publication number
EP0243557A1
EP0243557A1 EP86309286A EP86309286A EP0243557A1 EP 0243557 A1 EP0243557 A1 EP 0243557A1 EP 86309286 A EP86309286 A EP 86309286A EP 86309286 A EP86309286 A EP 86309286A EP 0243557 A1 EP0243557 A1 EP 0243557A1
Authority
EP
European Patent Office
Prior art keywords
aqueous solution
column
exchange resin
zeolite
cationic exchange
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP86309286A
Other languages
German (de)
French (fr)
Inventor
Anuj Kumar Saha
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
CBS Corp
Original Assignee
Westinghouse Electric Corp
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Westinghouse Electric Corp filed Critical Westinghouse Electric Corp
Publication of EP0243557A1 publication Critical patent/EP0243557A1/en
Withdrawn legal-status Critical Current

Links

Images

Classifications

    • G—PHYSICS
    • G21—NUCLEAR PHYSICS; NUCLEAR ENGINEERING
    • G21F—PROTECTION AGAINST X-RADIATION, GAMMA RADIATION, CORPUSCULAR RADIATION OR PARTICLE BOMBARDMENT; TREATING RADIOACTIVELY CONTAMINATED MATERIAL; DECONTAMINATION ARRANGEMENTS THEREFOR
    • G21F9/00—Treating radioactively contaminated material; Decontamination arrangements therefor
    • G21F9/04—Treating liquids
    • G21F9/06—Processing
    • G21F9/12—Processing by absorption; by adsorption; by ion-exchange

Definitions

  • This invention relates to an appartaus and method for removing strontium and/or cesium ions from an aqueous solution containing chemical hardness.
  • aqueous solutions of low level radioactive waste are treated using a combination of scavenging, precipitation, filtration, and ion exchange to reduce the radioactivity to a safe level.
  • This process has not proved to be entirely satisfactory because the chemical hardness in the solution interferes with the proper func­tioning of the organic ion exchange resin used to remove the radioactive ions.
  • a high sodium concentration in the waste solution also causes functional inefficiency in the organic ion exchanger.
  • the presence of phosphate ion greater than 0.5 ppm prevents the precipitation of calcium and magnesium ions during scavenging, and the presence of phosphate and other anions, such as chloride and sulfate, reduces the efficiency of the weak acid cationic exchange resin.
  • the removal of the strontium 90 ions in the solutions is not considered to be adequate.
  • the present invention resides in an apparatus for removing strontium and/or cesium ions from an aqueous solution containing chemical hardness characterised in that said appartaus comprises a first column containing an organic cationic exchange resin in alkali metal form; a second column containing erionite, chabazite, phillipsite, type A zeolite or mixtures of these zeolites; and means for passing said aqueous solution through said first column, then through said second column.
  • the invention also includes a method of removing radioactive strontium and/or cesium ions from an aqueous solution containing chemical hardness characterized by passing said aqueous solution through a first column containing an organic cationic exchange resin in alkali metal form; and passing said aqueous solution through a second column containing erionite, chabazite, phillipsite, and type A zeolite or mixtures of these zeolites.
  • All low radioactivity liquids including those of high hardness concentration and those that contain anions such as phosphate, fluoride, and sulfate, can be handled regardless of sodium ion concentration.
  • the decontamination factor can be increased by dividing the zeolite ion exchange bed into upper and lower portions, using a different mix of zeolites in each portion.
  • an aqueous solution containing radioactive ions enters filter 1 which removes any particulate matter that may be present.
  • the solution then passes through line 2, valve 3, line 4, and valve 5 into column 6 which contains an organic cationic exchange resin in alkali metal form (Na+ form).
  • the solution is atomized by atomizer 7 to help produce more surface area and thereby promote an intimate contact of the liquid and the solid resin bed.
  • the solution is atomized by atomizer 16, and leaves column 12 by line 17, passing through valve 18 into lines 19, valve 20, and line 21 for discharge. Should column 6 become exhausted or malfunction, valve 5 can be closed and valve 22 can be opened, permitting the aqueous solution to pass through line 23 into column 24 where it is atomized by atomizer 25. The aqueous solution then leaves column 24 by line 26 through valve 27 into line 28, valve 10, line 11, and into column 12. Aqueous solution leaving columns 6 and 24 can be tested for chemical hardness, and, if insufficient hardness has been removed, the solution can be recycled through valve 29 and line 30.
  • valve 10 can be closed and valve 31 can be opened, permitting the fluid to pass through line 32, and atomizer 33 into column 34, which is also filled with a specially selected zeolite, and is divided into upper portion 35 and lower portion 36, sepa­rated by liquid redistributor plate 37.
  • the aqueous solution leaves column 34 by line 38 and valve 39 into line 19.
  • Some low level radioactive waste solutions consist of evaporator condensates or overshoots (resulting from higher activity streams or evaporator malfunction) that contain very low or no chemical hardness. These condensates can enter the system by line 40. If chemical hardness is present, they can pass through line 41 and valve 42 into line 30 for treatment in column 6 or column 24. If chemical hardness is not present, valve 42 is closed and valve 43 is opened, and the condensate passes through line 44 and valve 45 through atomizer 46 into column 47, which is also packed with a specially selected zeolite, and is divided into an upper portion 48 and a lower portion 49, separated by liquid redistributor plate 50.
  • Condensate leaving column 47 by line 51 through valve 52 can be sent through lines 19 and 21 to discharge if the radioactivity is sufficiently low to meet the discharge limits. However, if any of the fluids leaving columns 47, 12, or 34 do not meet the discharge limits, valve 20 can be closed and valve 53 can be opened so that the fluids pass through line 54, which recycles them through columns 47, 12, or 34, until the radioactivity is reduced to the discharge limits. Should column 47 become exhausted or malfunction, valve 45 can be closed and valve 55 can be opened, and the condensate will pass through line 56 into column 34.
  • the waste water treated according to this inven­tion contains cesium and strontium ions and also contains chemical hardness such as calcium, magnesium, and/or iron ions.
  • the aqueous solution contains no particulate matter as it is removed by a filter that precedes treatment in the ion exchange columns.
  • the aqueous liquid also should not contain organic liquids as they interfere with the removal of radioactive ions from the solution. While any amount of cesium and strontium ions may be present, a typical low level waste solution will contain about 10 ⁇ 3 to about 10 microcuries per cubic centimeter and about 5 to about 1000 parts per million (ppm) of chemical hardness as calcium, magnesium, and iron.
  • the organic cationic exchange columns remove chemical hardness from the solution and reduce the solu­tion's conductivity. In addition, they also remove some of the strontium.
  • the organic cationic exchange resin must be in alkali metal from, preferably the sodium form, rather than the acid form, as the acid form is not effective in removing calcium. It is preferable to use a strong acid form rather than a weak acid form because a strong acid form is more durable and lasts longer.
  • a sulfonic acid based cationic exchange resin is preferable as it is readily available and works well. While either the gel or macroreticular type of exchange resin can be used, it is preferable to use a macroreticular exchange resin as that type of resin does not expand, is easier to work with, and is easier to dispose of.
  • phosphate ion is present in the aqueous solution, it is preferable to include about one to about 20 percent (all percentages herein are of weight unless otherwise specified) of an organic anionic ion exchange resin in with the organic cationic exchange resin in order to remove the phosphate ion. Also, as is shown in the drawing, it is preferable to use two columns so the process can continue by switching to a second column should one column become exhausted, plugged, or otherwise break down. The fluid leaving the organic cationic exchange column should be tested for calcium to determine when the column has become exhausted.
  • the aqueous solution is passed through a second type of column containing particular zeolites.
  • the zeolites that are used in this invention are erionite, chabazite, type A zeolite (a synthetic zeolite), and phil­lipsite. We have discovered that these particular zeolites have a higher capacity for removing cesium and strontium than do other ion exchange materials, such as organic cationic exchange resins.
  • the zeolites preferably have a pore size of about 4 to about 5 angstroms.
  • the second stage of the process is itself preferivelyably divided into two portions within the column.
  • the column is preferably divided to achieve a more selective Sr-90 partition/decontamination in the upper portion and more selective Cs-137 partition/decontamination in the lower portion.
  • the minimum packing height of the upper stage is preferably five feet.
  • the steam exiting the upper stage drop into a liquid redistributor plate, then trickles into the lower stage.
  • the upper portion contains a higher proportion of type A zeolite, which removes strontium better, and the lower portion contains a higher proportion of chabazite and/or erionite, which removes cesium better.
  • the upper stage preferably contains from 55 to 60% by volume type A zeolite and from 40 to 45% by volume chabazite and/or erionite.
  • the lower stage preferably contains from 25 to 30% by volume type A zeolite and from 70 to 75% by volume chabazite and/or erionite.
  • the ion exchange columns When the ion exchange columns are exhausted, they can be sluiced to a cement mixture where they are solidi­fied in cement, or otherwise disposed of.
  • This example shows the dynamic column test data obtained by passing a radioactive solution containing chemical hardness through an organic ion exchange prefilter and then through a zeolite bed.
  • the organic ion exchange bed removes chemical hardness (Ca++, Mg++, etc.) very effectively and at the same time decontaminates a very substantial quantity of Sr-90 and Cs-137.
  • the effluent from the organic ion-filter bed goes to the zeolite bed where the remaining traces of radioactivity is so effec­tively removed that the Cs-137 and Sr-90 levels of the effluent zeolite bed are undetectable. ( ⁇ 10 ⁇ 8uCi/c.c).
  • the organic ion exchange prefilter was strong acid cation exchange resin in Na+ form sold by Rohm & Hass under the trade designation IR-122.
  • the zeolite was erionite sold by Phelps dodge zeolites under the trade designation PDZ-50. The following tables give the conditions and results of this experiment.

Abstract

Apparatus for removing strontium and/or cesium ions from an aqueous solution containing chemical hardness. A first column containing an organic cationic exchange resin in alkali metal form removes the chemical hardness and some of the strontium and cesium ions, and a second column containing a zeolite which can be erionite, chabazite, phillipsite, type A zeolite, or mixtures there­of, removes radioactive ions. The apparatus also includes means for passing the aqueous solution through the first column then through the second column. Also a method for removing radioactive strontium and/or cesium ions from an aqueous solution containing chemical hardness by passing the aqueous solution through a first column containing an organic cationic exchange resin in alkali metal form and then passing the aqueous solution through a second column containing a zeolite which is erionite, chabazite, phillipsite, type A zeolite, or mixtures thereof.

Description

  • This invention relates to an appartaus and method for removing strontium and/or cesium ions from an aqueous solution containing chemical hardness.
  • At the present time, aqueous solutions of low level radioactive waste are treated using a combination of scavenging, precipitation, filtration, and ion exchange to reduce the radioactivity to a safe level. This process has not proved to be entirely satisfactory because the chemical hardness in the solution interferes with the proper func­tioning of the organic ion exchange resin used to remove the radioactive ions. A high sodium concentration in the waste solution also causes functional inefficiency in the organic ion exchanger. Also, the presence of phosphate ion greater than 0.5 ppm prevents the precipitation of calcium and magnesium ions during scavenging, and the presence of phosphate and other anions, such as chloride and sulfate, reduces the efficiency of the weak acid cationic exchange resin. Finally, the removal of the strontium 90 ions in the solutions is not considered to be adequate.
  • Accordingly, the present invention resides in an apparatus for removing strontium and/or cesium ions from an aqueous solution containing chemical hardness characterised in that said appartaus comprises a first column containing an organic cationic exchange resin in alkali metal form; a second column containing erionite, chabazite, phillipsite, type A zeolite or mixtures of these zeolites; and means for passing said aqueous solution through said first column, then through said second column.
  • The invention also includes a method of removing radioactive strontium and/or cesium ions from an aqueous solution containing chemical hardness characterized by passing said aqueous solution through a first column containing an organic cationic exchange resin in alkali metal form; and passing said aqueous solution through a second column containing erionite, chabazite, phillipsite, and type A zeolite or mixtures of these zeolites.
  • All low radioactivity liquids, including those of high hardness concentration and those that contain anions such as phosphate, fluoride, and sulfate, can be handled regardless of sodium ion concentration.
  • The decontamination factor can be increased by dividing the zeolite ion exchange bed into upper and lower portions, using a different mix of zeolites in each portion.
  • In order that the invention can be more clearly understood, convenient embodiments thereof will now be described, by way of example, with reference to the accom­panying drawing which is a flow diagram of an apparatus for removing strontium and/or cesium from an aqueous solution containing chemical hardness.
  • In the drawing, an aqueous solution containing radioactive ions, such as cesium and strontium, as well as chemical hardness, enters filter 1 which removes any particulate matter that may be present. The solution then passes through line 2, valve 3, line 4, and valve 5 into column 6 which contains an organic cationic exchange resin in alkali metal form (Na⁺ form). The solution is atomized by atomizer 7 to help produce more surface area and thereby promote an intimate contact of the liquid and the solid resin bed. The solution, with the chemical hardness and some of the radioactive ions removed, then passes through line 8, valve 9, valve 10, and line 11 into column 12, which is packed with a specially selected zeolite, and is divided into upper portion 13 and lower portion 14, sepa­rated by liquid redistributor plate 15. The solution is atomized by atomizer 16, and leaves column 12 by line 17, passing through valve 18 into lines 19, valve 20, and line 21 for discharge. Should column 6 become exhausted or malfunction, valve 5 can be closed and valve 22 can be opened, permitting the aqueous solution to pass through line 23 into column 24 where it is atomized by atomizer 25. The aqueous solution then leaves column 24 by line 26 through valve 27 into line 28, valve 10, line 11, and into column 12. Aqueous solution leaving columns 6 and 24 can be tested for chemical hardness, and, if insufficient hardness has been removed, the solution can be recycled through valve 29 and line 30. Should column 12 become exhausted or otherwise malfunction, valve 10 can be closed and valve 31 can be opened, permitting the fluid to pass through line 32, and atomizer 33 into column 34, which is also filled with a specially selected zeolite, and is divided into upper portion 35 and lower portion 36, sepa­rated by liquid redistributor plate 37. The aqueous solution, with its radioactivity removed, leaves column 34 by line 38 and valve 39 into line 19.
  • Some low level radioactive waste solutions consist of evaporator condensates or overshoots (resulting from higher activity streams or evaporator malfunction) that contain very low or no chemical hardness. These condensates can enter the system by line 40. If chemical hardness is present, they can pass through line 41 and valve 42 into line 30 for treatment in column 6 or column 24. If chemical hardness is not present, valve 42 is closed and valve 43 is opened, and the condensate passes through line 44 and valve 45 through atomizer 46 into column 47, which is also packed with a specially selected zeolite, and is divided into an upper portion 48 and a lower portion 49, separated by liquid redistributor plate 50. Condensate leaving column 47 by line 51 through valve 52 can be sent through lines 19 and 21 to discharge if the radioactivity is sufficiently low to meet the discharge limits. However, if any of the fluids leaving columns 47, 12, or 34 do not meet the discharge limits, valve 20 can be closed and valve 53 can be opened so that the fluids pass through line 54, which recycles them through columns 47, 12, or 34, until the radioactivity is reduced to the discharge limits. Should column 47 become exhausted or malfunction, valve 45 can be closed and valve 55 can be opened, and the condensate will pass through line 56 into column 34.
  • The waste water treated according to this inven­tion contains cesium and strontium ions and also contains chemical hardness such as calcium, magnesium, and/or iron ions. The aqueous solution contains no particulate matter as it is removed by a filter that precedes treatment in the ion exchange columns. The aqueous liquid also should not contain organic liquids as they interfere with the removal of radioactive ions from the solution. While any amount of cesium and strontium ions may be present, a typical low level waste solution will contain about 10⁻³ to about 10 microcuries per cubic centimeter and about 5 to about 1000 parts per million (ppm) of chemical hardness as calcium, magnesium, and iron.
  • The organic cationic exchange columns remove chemical hardness from the solution and reduce the solu­tion's conductivity. In addition, they also remove some of the strontium. The organic cationic exchange resin must be in alkali metal from, preferably the sodium form, rather than the acid form, as the acid form is not effective in removing calcium. It is preferable to use a strong acid form rather than a weak acid form because a strong acid form is more durable and lasts longer. A sulfonic acid based cationic exchange resin is preferable as it is readily available and works well. While either the gel or macroreticular type of exchange resin can be used, it is preferable to use a macroreticular exchange resin as that type of resin does not expand, is easier to work with, and is easier to dispose of. If phosphate ion is present in the aqueous solution, it is preferable to include about one to about 20 percent (all percentages herein are of weight unless otherwise specified) of an organic anionic ion exchange resin in with the organic cationic exchange resin in order to remove the phosphate ion. Also, as is shown in the drawing, it is preferable to use two columns so the process can continue by switching to a second column should one column become exhausted, plugged, or otherwise break down. The fluid leaving the organic cationic exchange column should be tested for calcium to determine when the column has become exhausted.
  • In the second stage of the process of this invention the aqueous solution is passed through a second type of column containing particular zeolites. The zeolites that are used in this invention are erionite, chabazite, type A zeolite (a synthetic zeolite), and phil­lipsite. We have discovered that these particular zeolites have a higher capacity for removing cesium and strontium than do other ion exchange materials, such as organic cationic exchange resins. The zeolites preferably have a pore size of about 4 to about 5 angstroms.
  • The second stage of the process is itself prefer­ably divided into two portions within the column. The column is preferably divided to achieve a more selective Sr-90 partition/decontamination in the upper portion and more selective Cs-137 partition/decontamination in the lower portion. The minimum packing height of the upper stage is preferably five feet. The steam exiting the upper stage drop into a liquid redistributor plate, then trickles into the lower stage. The upper portion contains a higher proportion of type A zeolite, which removes strontium better, and the lower portion contains a higher proportion of chabazite and/or erionite, which removes cesium better. By dividing the second stage into upper and lower stages, a higher decontamination factor (DF, equal to radioactivity before treatment divided by radioactivity after treatment) is obtained. The upper stage preferably contains from 55 to 60% by volume type A zeolite and from 40 to 45% by volume chabazite and/or erionite. The lower stage preferably contains from 25 to 30% by volume type A zeolite and from 70 to 75% by volume chabazite and/or erionite.
  • When the ion exchange columns are exhausted, they can be sluiced to a cement mixture where they are solidi­fied in cement, or otherwise disposed of.
  • The invention will now be illustrated with reference to the following Example.
    • EXAMPLE
  • This example shows the dynamic column test data obtained by passing a radioactive solution containing chemical hardness through an organic ion exchange prefilter and then through a zeolite bed. The organic ion exchange bed removes chemical hardness (Ca⁺⁺, Mg⁺⁺, etc.) very effectively and at the same time decontaminates a very substantial quantity of Sr-90 and Cs-137. The effluent from the organic ion-filter bed goes to the zeolite bed where the remaining traces of radioactivity is so effec­tively removed that the Cs-137 and Sr-90 levels of the effluent zeolite bed are undetectable. (<10⁻⁸uCi/c.c). The organic ion exchange prefilter was strong acid cation exchange resin in Na⁺ form sold by Rohm & Hass under the trade designation IR-122. The zeolite was erionite sold by Phelps dodge zeolites under the trade designation PDZ-50. The following tables give the conditions and results of this experiment.
    Figure imgb0001
    Figure imgb0002

Claims (13)

1. Apparatus for removing strontium and/or cesium ions from an aqueous solution containing chemical hardness characterized in that said appartaus comprises a first column containing an organic cationic exchange resin in alkali metal form; a second column containing erionite, chabazite, phillipsite, type A zeolite or mixtures of these zeolites; and means for passing said aqueous solution through said first column, then through said second column.
2. Apparatus according to claim 1 characterized in that the aqueous solution is radioactive to the extent of from 10⁻³ to 10 microcuries/cc, and contains from 5 to 1000 ppm of calcium, magnesium or iron ion.
3. Apparatus according to claim 1 or 2, charac­terized in that the alkali metal is sodium.
4. Apparatus according to claim 1, 2 or 3, characterized in that the organic cationic exchange resin is a strong acid type.
5. Apparatus according to claim 4, characterized in that the organic cationic exchange resin is sulfonic acid based.
6. Apparatus according to any of claims 1 to 5, characterized in that the organic cationic exchange resin is a macroreticular type.
7. Apparatus according to any of claims 1 to 6, characterized in that the aqueous solution includes phos­phate ion and the organic cationic exchange resin is mixed with from 1 to 20% organic anionic exchange resin.
8. Apparatus according to any of claims 1 to 7, characterized in that said apparatus includes means for testing said aqueous solution for calcium ions after it has passed through said first column, and for recycling it through said organic cationic exchange resin bed if signif­icant concentrations of calcium ions are present.
9. Apparatus according to any of claims 1 to 8, characterized in that said apparatus includes means for atomizing the aqueous solution as it enters the first and second columns.
10. Apparatus according to any of claims 1 to 9, characterized in that said apparatus includes means for filtering the aqueous solution before it enters said first column.
11. Apparatus according to any of claims 1 to 10, characterized in that the second column is divided into an upper portion and a lower portion, and in said upper portion are from 55 to 60% by volume type A, zeolite and from 40 to 45% by volume chabazite, erionite, phillipsite or mixtures thereof, and in said lower portion are from 25 to 30% by volume type A zeolite and from 70 to 75% by volume chabazite, erionite, phillispsite or mixtures thereof.
12. Apparatus according to any of claims 1 to 11, characterized in that the zeolite has pore size of from 4 to 5 angstroms.
13. A method of removing radioactive strontium and/or cesium ions from an aqueous solution containing chemical hardness characterized by passing said aqueous solution through a first column containing an organic cationic exchange resin in alkali metal form; and passing said aqueous solution through a second column containing erionite, chabazite, phillipsite, and type A zeolite or mixtures of these zeolites.
EP86309286A 1986-04-30 1986-11-27 Apparatus and method for removing strontium and/or cesium ions from an aqueous solution containing chemical hardness Withdrawn EP0243557A1 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US857677 1977-12-05
US85767786A 1986-04-30 1986-04-30

Publications (1)

Publication Number Publication Date
EP0243557A1 true EP0243557A1 (en) 1987-11-04

Family

ID=25326506

Family Applications (1)

Application Number Title Priority Date Filing Date
EP86309286A Withdrawn EP0243557A1 (en) 1986-04-30 1986-11-27 Apparatus and method for removing strontium and/or cesium ions from an aqueous solution containing chemical hardness

Country Status (3)

Country Link
EP (1) EP0243557A1 (en)
JP (1) JPS62262784A (en)
KR (1) KR870010563A (en)

Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1990009026A1 (en) * 1989-01-31 1990-08-09 Franz Roiner Process for decontaminating materials that have been attacked by metallic ions or by radioactive substances
ES2046947A1 (en) * 1992-05-13 1994-02-01 Univ La Laguna Residual water treatment
CN104054137A (en) * 2012-01-18 2014-09-17 大日精化工业株式会社 Method for removing radioactive cesium, hydrophilic resin composition for removing radioactive cesium, method for removing radioactive iodine and radioactive cesium, and hydrophilic resin composition for removing radioactive iodine and radioactive cesium
JP2015017003A (en) * 2013-07-09 2015-01-29 富士チタン工業株式会社 Artificial zeolite excellent in adsorption capacity of both of cesium and strontium and production method of the same
EP2556511A4 (en) * 2010-03-09 2015-03-04 Kurion Inc Isotope-specific separation and vitrification using ion-specific media
JP2015052522A (en) * 2013-09-06 2015-03-19 株式会社荏原製作所 Device and method for decontaminating waste water including radioactive cesium and salt
US9365911B2 (en) 2012-03-26 2016-06-14 Kurion, Inc. Selective regeneration of isotope-specific media resins in systems for separation of radioactive isotopes from liquid waste materials
RU168418U1 (en) * 2016-08-08 2017-02-02 Общество с ограниченной ответственностью Научно-производственное предприятие "Эксорб" Device for cleaning solutions from radionuclides
RU2672662C2 (en) * 2016-05-11 2018-11-19 Общество с ограниченной ответственностью "Акватория" Method for cleaning salt solutions from radionuclides and installation for its implementation
US10183870B2 (en) 2015-05-22 2019-01-22 Access Business Group International Llc Point-of-use water treatment system

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
TWI516451B (en) * 2009-01-12 2016-01-11 通路實業集團國際公司 Point-of-use water treatment system
JP5909096B2 (en) * 2012-01-17 2016-04-26 三菱重工業株式会社 Radioactive liquid processing equipment
JP2014048168A (en) * 2012-08-31 2014-03-17 Fuji Electric Co Ltd Radioactive contaminant decontamination method and device
JP6175354B2 (en) * 2013-11-05 2017-08-02 太平洋セメント株式会社 Method and apparatus for treating contaminated water
KR101551233B1 (en) * 2014-09-16 2015-09-10 한국원자력연구원 Treatment method for radioactive wastewater generated in severe accident in nuclear power plant

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DD78224A (en) *
US2752309A (en) * 1952-04-30 1956-06-26 Ardath H Emmons Process for water decontamination
FR1399711A (en) * 1964-04-09 1965-05-21 Kuhlmann Ets Decontamination process for a radioactive solution
DE1517610A1 (en) * 1964-05-21 1970-01-29 Planungs Und Forschungsgesells Method and device for removing radioactive cations from soft surface water in large-scale supply operations with rapid filter systems, in particular for the supply of drinking water from reservoirs and natural standing waters
FR2310616A1 (en) * 1975-05-07 1976-12-03 Shin Tohoku Chemical Ind Co Lt RADIO-ACTIVE WASTE WATER TREATMENT PROCESS
EP0117315A1 (en) * 1983-02-11 1984-09-05 The Dow Chemical Company Method for removing cesium from an aqueous liquid, method for purifying the reactor coolant in boiling water and pressurized water reactors and a mixed ion exchanged resin bed, useful in said purification

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DD78224A (en) *
US2752309A (en) * 1952-04-30 1956-06-26 Ardath H Emmons Process for water decontamination
FR1399711A (en) * 1964-04-09 1965-05-21 Kuhlmann Ets Decontamination process for a radioactive solution
DE1517610A1 (en) * 1964-05-21 1970-01-29 Planungs Und Forschungsgesells Method and device for removing radioactive cations from soft surface water in large-scale supply operations with rapid filter systems, in particular for the supply of drinking water from reservoirs and natural standing waters
FR2310616A1 (en) * 1975-05-07 1976-12-03 Shin Tohoku Chemical Ind Co Lt RADIO-ACTIVE WASTE WATER TREATMENT PROCESS
EP0117315A1 (en) * 1983-02-11 1984-09-05 The Dow Chemical Company Method for removing cesium from an aqueous liquid, method for purifying the reactor coolant in boiling water and pressurized water reactors and a mixed ion exchanged resin bed, useful in said purification

Cited By (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1990009026A1 (en) * 1989-01-31 1990-08-09 Franz Roiner Process for decontaminating materials that have been attacked by metallic ions or by radioactive substances
ES2046947A1 (en) * 1992-05-13 1994-02-01 Univ La Laguna Residual water treatment
US9437336B2 (en) 2010-03-09 2016-09-06 Kurion, Inc. Isotope-specific separation and vitrification using ion-specific media
US10020085B2 (en) 2010-03-09 2018-07-10 Kurion, Inc. Isotope-specific separation and vitrification
EP2556511A4 (en) * 2010-03-09 2015-03-04 Kurion Inc Isotope-specific separation and vitrification using ion-specific media
EP2806426A4 (en) * 2012-01-18 2015-12-16 Dainichiseika Color Chem Method for removing radioactive cesium, hydrophilic resin composition for removing radioactive cesium, method for removing radioactive iodine and radioactive cesium, and hydrophilic resin composition for removing radioactive iodine and radioactive cesium
CN104054137A (en) * 2012-01-18 2014-09-17 大日精化工业株式会社 Method for removing radioactive cesium, hydrophilic resin composition for removing radioactive cesium, method for removing radioactive iodine and radioactive cesium, and hydrophilic resin composition for removing radioactive iodine and radioactive cesium
CN104054137B (en) * 2012-01-18 2016-09-07 大日精化工业株式会社 The removing method of radiocesium, for removing the removing method of hydrophilic resin oil/fat composition, radioiodine and the radiocesium of radiocesium and for removing the hydrophilic resin oil/fat composition of radioiodine and radiocesium
US9365911B2 (en) 2012-03-26 2016-06-14 Kurion, Inc. Selective regeneration of isotope-specific media resins in systems for separation of radioactive isotopes from liquid waste materials
US9714457B2 (en) 2012-03-26 2017-07-25 Kurion, Inc. Submersible filters for use in separating radioactive isotopes from radioactive waste materials
US10480045B2 (en) 2012-03-26 2019-11-19 Kurion, Inc. Selective regeneration of isotope-specific media resins in systems for separation of radioactive isotopes from liquid waste materials
JP2015017003A (en) * 2013-07-09 2015-01-29 富士チタン工業株式会社 Artificial zeolite excellent in adsorption capacity of both of cesium and strontium and production method of the same
JP2015052522A (en) * 2013-09-06 2015-03-19 株式会社荏原製作所 Device and method for decontaminating waste water including radioactive cesium and salt
US10183870B2 (en) 2015-05-22 2019-01-22 Access Business Group International Llc Point-of-use water treatment system
RU2672662C2 (en) * 2016-05-11 2018-11-19 Общество с ограниченной ответственностью "Акватория" Method for cleaning salt solutions from radionuclides and installation for its implementation
RU168418U1 (en) * 2016-08-08 2017-02-02 Общество с ограниченной ответственностью Научно-производственное предприятие "Эксорб" Device for cleaning solutions from radionuclides

Also Published As

Publication number Publication date
KR870010563A (en) 1987-11-30
JPS62262784A (en) 1987-11-14

Similar Documents

Publication Publication Date Title
EP0243557A1 (en) Apparatus and method for removing strontium and/or cesium ions from an aqueous solution containing chemical hardness
Pansini Natural zeolites as cation exchangers for environmental protection
US2752309A (en) Process for water decontamination
CA2101261C (en) Method of composite sorbents manufacturing
EP0118493B1 (en) Fixation of anionic materials with a complexing agent
Harjula et al. Removal of radioactive cesium from nuclear waste solutions with the transition metal hexacyanoferrate ion exchanger CsTreat
US4853130A (en) Method for purifying liquids
US6991731B2 (en) Treatment process for removing radioactive thorium from solvent extraction liquid effluent
EP0555996B1 (en) Methods and apparatus for treating aqueous indutrial effluent
JPH0247599A (en) Treatment method for radioactive nuclide containing waste liquid
JPH0327264B2 (en)
US2373632A (en) Removal of fluorine from water
JPH0319520B2 (en)
JPS6334999B2 (en)
US5879433A (en) Method and apparatus for reducing the acid gas and/or inert particulate content of steam
US4927796A (en) Compositions for purifying liquids
JP2001212455A (en) Treating device for discharge water containing boron and treating method therefor
RU2055814C1 (en) Having nitrogen-bearing components and heavy metals minerals-free sewage purification method
US3660283A (en) Method for regenerating cation exchange resin
US4654146A (en) Ion exchanger to separate heavy alkali metal ions
Campbell et al. Low-level liquid waste decontamination by ion exchange
Park et al. An experimental study on liquid radioactive waste treatment process using inorganic ion exchanger
RU2050027C1 (en) Process of decontamination of solutions from radionuclides
Chibi et al. A promising approach to fluoride removal in rural drinking water supplies
DE3513943C2 (en)

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): DE ES FR GB IT SE

17P Request for examination filed

Effective date: 19880428

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE APPLICATION IS DEEMED TO BE WITHDRAWN

18D Application deemed to be withdrawn

Effective date: 19890531

RIN1 Information on inventor provided before grant (corrected)

Inventor name: SAHA, ANUJ KUMAR