Concentrate treatment system

• US 8,753,518 B2
• Filed: 09/25/2011
• Issued: 06/17/2014
• Est. Priority Date: 10/15/2010
• Status: Active Grant

• Current Assignee: AVANTech, LLC
• Original Assignee: Diversified Technologies Services, Inc.
• Inventors: Brunsell, Dennis A., Jensen, Charles E., Beets, Larry E.
• Primary Examiner(s): Nguyen, Nam
• Assistant Examiner(s): GURTOWSKI, RICHARD C
• Application Number:
  US13/820,145
• Publication Number:
  US 20130153473A1
• Time in Patent Office: 996 Days
• Field of Search: None
• US Class Current: 210/721
• CPC Class Codes: A62D 3/38 by oxidation; by combustion
• CPC Class Codes: C02F 1/04 by distillation or evaporation
• CPC Class Codes: C02F 1/28 by sorption using ion-exchange C02F1/42; sorbent compositions B01J
• CPC Class Codes: C02F 1/38 by centrifugal separation
• CPC Class Codes: C02F 1/42 by ion-exchange ion-exchange in general B01J
• CPC Class Codes: C02F 1/444 by ultrafiltration or microfiltration
• CPC Class Codes: C02F 1/66 by neutralisation; pH adjustment for degassing C02F1/20; using ion-exchange C02F1/42; for flocculation or precipitation of suspended impurities C02F1/52; for removing dissolved compounds C02F1/58
• CPC Class Codes: C02F 1/722 Oxidation by peroxides
• CPC Class Codes: C02F 1/74 with air aeration of stretches of water C02F7/00
• CPC Class Codes: C02F 1/76 with halogens or compounds of halogens C02F1/4674 takes precedence
• CPC Class Codes: C02F 1/78 with ozone C02F1/4672 takes precedence
• CPC Class Codes: C02F 11/12 by de-watering, drying or thickening
• CPC Class Codes: C02F 2001/007 Processes including a sedimentation step
• CPC Class Codes: C02F 2101/006 Radioactive compounds
• CPC Class Codes: C02F 2209/005 Processes using a programmable logic controller [PLC]
• CPC Class Codes: C02F 2209/008 comprising telecommunication features, e.g. modems or antennas
• CPC Class Codes: C02F 2209/02 Temperature
• CPC Class Codes: C02F 2209/04 Oxidation reduction potential [ORP]
• CPC Class Codes: C02F 2209/06 pH
• CPC Class Codes: C02F 2303/12 Prevention of foaming
• CPC Class Codes: C02F 9/00 : Multistage treatment of water, waste water or sewage
• CPC Class Codes: G21C 19/46 : Aqueous processes , e.g. by using organic extraction means, including the regeneration of these means
• CPC Class Codes: G21F 9/12 : by absorption; by adsorption; by ion-exchange
• CPC Class Codes: G21F 9/125 : by solvent extraction
• CPC Class Codes: Y02E 30/30 : Nuclear fission reactors
• CPC Class Codes: Y02W 30/50 : Reuse, recycling or recovery technologies

Abstract

In one aspect the invention provides a system for treating a wastestream, particularly a radwaste, for safe disposal and, in final processing converting it into one or both forms including an aqueous form for safe discharge to the environment and a solidified form for safe disposal. In another aspect the invention provides the capacity to employ a step where a specific target element strategy can be set up synchronizing sorbent substance choices and multiple recycle options to remove target substances from wastestream as a part of its Sorption or Powder Sorbent Isotopic Reduction step (II). Other steps cooperate with Sorption step (II) including Oxidation (I), Solid-Liquid separation (III), and Selective Ion Exchange (IV) to deliver the wastestream to final processing.

Claims

1. A system for treating a liquid or aqueous wastestream consisting of at least one of a group of wastes consisting of radioactive concentrate fluid, historic waste and other forms of environmental or hazardous waste or radwaste;

and converting the wastestream into at least one of two selected forms including a form which can be solidified, or solidified form, for safe disposal and an aqueous form which can be safely discharged to the environment, said system comprising the steps, designated as Roman numerals;

I, II, III, IV and V, of;

(I) oxidizing the wastestream such that any existing chelant material or substance contained in the wastestream is substantially rendered non-effective as a chelant of metals or destroyed thereby releasing the metals into ionic form, and the wastestream is rendered subject to, or permissive of, precipitation of cobalt and other metals and release of other isotopes for removal;

(II) mixing the wastestream with at least one target Sorbent material for Isotopic Reduction;

(III) separating the wastestream into Solid and Liquid components;

(IV) treating the wastestream by Selective Ion exchange (IX); and

(V) final processing, wherein at least one step is chosen from a group consisting of;

(Va) discharging the wastestream in said aqueous form, and

(Vb) drying of a resulting wastestream having dissolved solids to Dry Solids, as said solidified form.

2. The system of claim 1, wherein, step (I) is cycled through at least one operation selected from a group of operations consisting of:

batch operation and continuous operation.

3. The system of claim 2, wherein, the operation has a time magnitude of from about one (1) hour to about forty-eight (48) hours.

4. The system of claim 2, wherein, as a part of step (I) the wastestream is conveyed or transferred from a stored location (6) to a recycle oxidation vessel (12).

5. The system of claim 4, wherein, during a contemporaneous period of time during or after said wastestream being conveyed or transferred the wastestream is recycled from and returning to the recycle oxidation vessel (12), said oxidation vessel (12) being selectively served by a means of providing heat exchange (18) when required to adjust the temperature to a more favorable oxidation range;

and wherein a pH and temperature measurement area (13) and ORP measurement station (11) are utilized for measurement purposes to determine further treatment required.

6. The system of claim 5, wherein, pH is determined and adjustment performed using a means for chemical injection (15).

7. The system of claim 5, wherein, an antifoaming agent is utilized, said agent being provided through the means for chemical injection (15).

8. The system of claim 6, wherein, the pH is below about 12.5.

9. The system of claim 6, wherein, the pH is less than about 12.

10. The system of claim 7, wherein, the ORP is from about +300 mV to about +1000 mV after adjustment for the pH.

11. The system of claim 5, wherein the means of providing heat exchange (18) operates to lower the temperature of the wastestream to a temperature of less than about 80 degrees F. or about 26.67 degrees C.

12. The system of claim 5, wherein the means of providing heat exchange (18) operates to lower the temperature of the wastestream to a temperature of less than or equal to about 60 degrees F. or about 15.56 degrees C.

29. The system in accordance with claim 1, wherein, said step (I) being an ozone oxidation step, wherein the wastestream being recycled for temperature and pH adjustment, and ORP measurement in relation to the temperature or pH, to and from a recycle oxidation vessel (12);

wherein, the temperature in step (I) is maintained through adjustment in a range of from about 20 degrees C. to about 25 degrees C.;

pH in step (I) is maintained through adjustment in a range of from about 11 to about 12; and

, wherein, the ORP is in a range of from about +500 mV to about +1000 mV, for indication that chelant oxidation processing is occurring; and

wherein, said step (II) of the system further comprising means for sequentially and selectively recycling the aqueous wastestream through multiple recycle lines such that one and multiple sorbent materials can be added to a sorbent container (20) to target existing radioisotopes when present.

13. A system for treating a liquid or aqueous wastestream (8) consisting of at least one of a group of wastes consisting of radioactive concentrate fluid, historic waste and other forms of environmental or hazardous waste or radwaste;

and converting the wastestream into at least one of two selected forms consisting of a form which can be evaporated to a solid, or solidified form, which can be safely discharged to an industrial or plant facility and an aqueous form which can be safely discharged to the environment;

said system comprising the steps, designated as Roman numerals;

I, II, III, IV and V, of;

(I) oxidizing the wastestream such that any existing chelant material, or substance contained in the wastestream is substantially rendered non-effective as a chelant of metals or destroyed, and the wastestream is rendered subject to, or permissive of, precipitation of cobalt and other metals and release of other isotopes for removal or ion exchange;

(II) mixing the wastestream with at least one target Sorbent material for Isotopic Reduction;

(III) separating the wastestream into Solid and Liquid components;

(IV) treating the wastestream by Selective Ion exchange (IX), and

(V) final processing, wherein at least one step is chosen from a group consisting of;

(Va) discharging the wastestream in said aqueous form, and

(Vb) drying of a resulting wastestream having dissolved solids to Dry Solids, as said solidified form.

14. The system of claim 13, wherein, step (I) is an Oxidation or Ozone Oxidation step, further comprising the substeps of:

communicating the wastestream (8) from a facility or storage area (6) through a means for solids separation (7), whereat a solids portion of the wastestream is conveyed to a solids collection tank (28), and a remaining part of the wastestream is conveyed to a recycle oxidation vessel (12) for processing therein,

conveying the wastestream after processing in the recycle oxidation vessel (12) to a means for measuring pH and temperature (13), and further through a means for providing ORP measurement (11), and

transferring at least part of the wastestream to a means for providing heat exchange (18), the means (18) communicating with an eductor supply feed (19) and the means for providing ozone eductor and mixing (16b) through which the wastestream is communicated to an oxidation return line (14a) back in recycle to the vessel (12), said line (14a) further communicating with and being contemporaneously served by a means for selectively providing chemical injection (15).

15. The system of claim 14, wherein, step (II) is a Sorption or Powder Sorbent Isotopic Reduction step, further comprising the substeps of:

marshaling at least a part of the remaining wastestream not being transferred to the means for providing heat exchange (18), and transferring the remaining wastestream to a sorbent treatment area (20),

selecting at least one sorbent substance when it is desired to remove at least one subject target element or isotope forming a part of the wastestream transferred to the sorbent treatment area (20), adding the at least one sorbent substance selected to the treatment area (20) and mixing it therewithin, and coordinating at least one further substep selected from a group comprising repeating the selecting at least one sorbent substance until sufficient time has passed to substantially absorb the target element or isotope forming a part of the wastestream, and recycling the wastestream transferred to the sorbent treatment area (20) until sufficient time has passed to substantially absorb the target element or isotope forming a part of the wastestream, wherein said at least one sorbent substance is selected from a group consisting of powdered, granular, liquid ionic flocculent and other forms of sorbents;

communicating the wastestream from the area (20) to a means for separation and settling (33), wherein at least a portion of the wastestream is separated out to a solid material, and wherein, between the sorbent treatment area (20) and the means for separation and settling (33) communicating a first means (22A, 38), for selectable recycle to the treatment area (20), when selected, of a portion of the wastestream chosen not to pass through the means for separation and settling (33),

transferring the solid material from the separation and settling means (33) to the collection tank (28), and transferring the remaining wastestream from the means (33) to a filter unit (34), and wherein, between the separation and settling means (33) and the filter unit (34) communicating a second means (31A, 38) for selectable recycle to the treatment area (20), when selected, of a portion of the wastestream chosen not to pass through the filter unit (34).

16. The system of claim 15, wherein as a part of step (II), one sorbent material is added and mixed (24, 24a) in the sorbent treatment area (20), and the first means (22A, 38) for selectable recycle to the treatment area (20) being selected and repeated when necessary until sufficient time has passed to substantially absorb the at least one subject target element.

17. The system of claim 15, wherein as a part of step (II), the second means (31A, 38) for selectable recycle being utilized for removal of sorbents and other solids without passing such materials through the filter unit (34), and being utilized when a sorbent currently being used is required to be removed prior to a subsequent sorbent being added to the sorbent treatment area (20).

18. The system of claim 15, wherein, step (III) is a Solid-Liquid Separation step further comprising the substeps of:

filtering the remaining wastestream through a filter media (35) of the filter unit (34),

communicating with a rejected side of the filter media (35) a third means (36A, 38) for selectable recycle to the treatment area (20), for recycling at least a part of the wastestream, not passing through the media (35), to the sorbent treatment area (20), and

contemporaneously directing at least a part of the wastestream, passing through the media (35) to a manifold system (41).

19. The system of claim 18, wherein the wastestream processes through the means for separation and settling (33) and to the filter unit (34), and wherein a reject portion from the reject side of the filter media (35) of the filter unit (34) being returned through the third means (36A, 38) for selectable recycle to the treatment area (20) for further processing.

20. The system of claim 18, wherein, when no solids are present in the wastestream and no need to remove solids prior to passage through sorbent treatment area (20), and only one sorbent is utilized in the sorbent treatment area (20), the first means for selectable recycle (22A, 38) and the third means for selectable recycle (36A, 38), to the treatment area (20) being utilized.

21. The system of claim 18, wherein, when at least two separate processing passes through the sorbent treatment area (20) are selected and utilized or a first sorbent is removed from the treatment area (20) before adding and using a second or respective additional sorbent, for absorption of targeted element substances, then the second means for selectable recycle (31A, 38), to the treatment area (20) being utilized.

22. The system of claim 18, wherein, adding one and more than one sorbents to the sorbent treatment area (20) in a manner selected to address sorbency-targeting of one and more than one of said subject target element or isotope, and such that said adding of respective individual sorbents when chosen creates a sequential adding of sorbents and sorbent addition strategy to best absorb the subject target element in the treatment area (20), and when present more than one such subject target element, during related or contemporaneous time periods while the subject target element of interest is present in the treatment area (20).

23. The system of claim 18, wherein, step (IV) is an Adjustable and Configurable Ion exchange (IX) step further comprising:

processing the wastestream passing into the manifold system (41) by selective removal of isotopes, wherein the system (41) comprises at least one vessel unit (42) for ion exchange, the unit (42) being served and connected to at least one manifold line (43), and wherein one and more such vessels are selectively deployable in series, and adjustable and configurable through bypass function, in determining flow path and selective IX treatment through the system (41), and

exiting the remaining wastestream from the system (41) to a means of IX effluent conveyance (51).

24. The system of claim 23, wherein, as a part of said step (V), the substeps comprise:

conveying the remaining wastestream on the conveyance (51) to a means for storing and monitoring fluid (50),

passing at least a portion of the remaining wastestream from the means (50) to at least one of the group consisting of;

the Water Discharge (Va), and

the Drying of resulting wastestream dissolved solids (Vb); and

contemporaneously guiding at least a part of the remaining wastestream through a recycling subprocess where the wastestream is returned to the means for storing and monitoring fluid (50).

25. The system of claim 24, wherein:

the Water Discharge (Va) comprises at least a means for discharging the remaining wastestream as clean water to the environment; and

the Drying (Vb) comprises at least a means for providing evaporator feed conveyance (53) of at least a part of the remaining wastestream from the means (50), a means for evaporation (54) in communication with the means (53), and a means connected to the evaporation (54) for selective recycle back to the facility or storage area (6).

26. The system of claim 25, wherein:

the recycling subprocess comprises at least;

a means (50R) for communicating and transferring the at least part of the remaining wastestream from the means for storing and monitoring fluid (50) to the means of IX effluent conveyance (51),

means for providing pH adjustment in communication with the means of conveyance (51), and

means of measuring pH, in communication with the conveyance (51), before the wastestream is transferred to the IX effluent conveyance (51) and returned to the means for storing and monitoring fluid (50).

27. The system of claim 18, wherein the system is coordinated and controlled as to each process step by means for integrated remote computer system control.

30. The system in accordance with claim 14, wherein, the temperature in step (I) being maintained through adjustment in a range of from about 20 degrees C. to about 25 degrees C.;

pH in step (I) is maintained through adjustment in a range of from about 11 to about 12; and

, wherein, the ORP is in a range of from about +500 mV to about +1000 mV, for indication that chelant oxidation processing is occurring.

28. A system for treating a liquid or aqueous wastestream, when internally enclosed within a treatment environment, the wastestream consisting of at least one of a group of wastes consisting of radioactive concentrate fluid, historic waste and other forms of environmental or hazardous waste or radwaste;

and converting the wastestream into at least one of two selected forms including a form which can be evaporated to a solid, or solidified form, which can be safely discharged to an industrial or plant facility, and an aqueous form which can be safely discharged to the environment, said system comprising the steps of;

(I) oxidizing the wastestream through a factor of pH adjustment such that any existing chelant material, or substance thereof, is substantially rendered non-effective as a chelant of metals or destroyed, whereby pH is lowered and rendered substantially unchanging and CO2 is produced, and the wastestream is rendered subject to or permissive of, by virtue of the absence of binding chelant, precipitation of cobalt and other metals and release of other isotopes for removal or ion exchange;

(II) mixing the wastestream with at least one target Sorbent material for Isotopic Reduction;

(III) separating the wastestream into Solid and Liquid components;

(IV) treating the wastestream by Selective Ion exchange (IX); and

(V) final processing, wherein at least one step is chosen from a group consisting of;

(Va) discharging the wastestream in said aqueous form, and

(Vb) drying of a resulting wastestream having dissolved solids to Dry Solids, as said solidified form.

31. The system in accordance with claim 28;

wherein, step (I) using an ozone oxidation with recycling to a recycle oxidation vessel (12);

wherein, a temperature range being used in step (I) being in a range of from about 20 degrees C. to about 25 degrees C.;

the pH in step (I) being maintained in a range of from about 11 to about 12; and

, wherein, the ORP, when measured, is in a range of from about ±

500 mV to about +1000 mV, for indication that chelant oxidation processing is occurring.

36. The system in accordance with claim 31 wherein, contemporaneous to a time when the CO2 is produced a change in pH of about 0.01 to about 0.1 being utilized to determine that greater than about 99.9% of the chelant has been broken into smaller pieces which can no longer chelate the Cobalt and other metals and the release of other isotopes, such that removal thereof in the system being carried out by the steps (II), (III) and (IV).

32. A system for treating a liquid or aqueous wastestream comprising at least one of a group of wastes consisting of radioactive concentrate fluid, historic waste and other forms of environmental or hazardous waste or radwaste product from a nuclear facility;

inherently containing when present, without specific addition, chelant and organics; and

converting the wastestream into at least one of two selected forms including a form which can be solidified, or solidified form, for safe disposal and an aqueous form which can be safely discharged to the environment, the system comprising the steps designated as Roman numerals;

I, II, III, IV and V, of;

(I) ozone oxidizing the wastestream through temperature mediated ozonation in a temperature range of from about 55 degrees F., or about 12.7 degrees C., to about less than or equal to about 65 degrees F., or 18.3 degrees C., such that any existing chelant chemical compound or organic substance contained in the wastestream is substantially rendered non-effective as a chelant of metals or destroyed thereby releasing the metals into ionic form for treatment in the system with the steps II, III, IV and V;

(II) mixing the wastestream with at least one target Sorbent material for Isotopic Reduction;

(III) separating the wastestream into Solid and Liquid components;

(IV) treating the wastestream by Selective Ion exchange (IX); and

(V) final processing, wherein at least one step is chosen from a group consisting of;

(Va) discharging the wastestream in said aqueous form, and

(Vb) drying of a resulting wastestream having dissolved solids to Dry Solids, as said solidified form.

33. The system of claim 32 wherein, as a part of step (I) the wastestream being conveyed or transferred from a stored location (6) to a recycle oxidation vessel (12);

the vessel (12) being served by a means for recycle;

said means for recycle having an oxidation recycle line (22) passing out of and returning to the vessel (12); and

, wherein, during a contemporaneous period of time during or after said wastestream being conveyed or transferred to the vessel (12) the wastestream being recycled within the means for recycle in the line (22), said means for recycle having a ozone supply skid or module (16a) and a heat exchanger (18) for adjustment when required of the temperature to the temperature range of the ozone oxidizing, for more favorable oxidation range and more efficient use of ozone in the ozone oxidation in step (I) of any chelant present; and

wherein means for recycle having a pH and temperature measurement area (13) and ORP measurement station (11) being utilized for measurement purposes to determine further treatment required, such that pH can be adjusted and retained to less than about 12.0 and ORP can be retained within a range of from about +300 mV to about +1000 mV by virtue of mediation of temperature and pH.

34. The system of claim 33, wherein, the means for recycle further having a chemical injection skid (15), the injection skid (15) being used for adjustment of pH when needed.

35. The system of claim 33, wherein the system being enhanced and controlled in step (II) through substantially eliminating foam generated during processing.

37. The system of claim 34, wherein, chelant and organics, when present, being one or more of a group consisting of:

EDTA, citric acid, oxalic acid, LOMI solution, and other chelants.

38. The system of claim 32, wherein, step (I) further comprising the substeps of:

communicating the wastestream (8) from a facility or storage area (6) through a means for solids separation (7), whereat a solids portion of the wastestream is conveyed to a solids collection tank (28), and a remaining part of the wastestream is conveyed to a recycle oxidation vessel (12) for processing therein,

conveying the wastestream after processing in the recycle oxidation vessel (12) to a means for measuring pH and temperature (13), and further through a means for providing ORP measurement (11), and adjusting when needed to maintain the pH at less than about 12 and the ORP at a value within a range of from about +300 mV to about +1000 mV, and

transferring at least part of the wastestream through an oxidation recycle line (22) to a means for providing heat exchange (18), the means (18) communicating with an educator supply feed (19) and a means for providing ozone educator and mixing (16b) through which the wastestream is communicated to an oxidation return line (14a), which is an extension and part of the oxidation recycle line (22), back in recycle to the vessel (12), said line (14a) further communicating with and being contemporaneously served by a means for selectively providing chemical injection (15) for chemically adjusting the pH and the ORP.

39. The system of claim 38, wherein, step (II) is a Sorption or Powder Sorbent Isotopic Reduction step, further comprising the substeps of:

marshaling at least a part of the remaining wastestream not being transferred to the means for providing heat exchange (18), and transferring the remaining wastestream to a sorbent treatment area (20),

selecting at least one sorbent substance when it is desired to remove at least one subject target element or isotope forming a part of the wastestream transferred to the sorbent treatment area (20), adding the at least one sorbent substance selected to the treatment area (20) and mixing it therewithin, and coordinating at least one further substep selected from a group comprising;

repeating the selecting at least one sorbent substance until sufficient time has passed to substantially absorb the target element or isotope forming a part of the wastestream, and recycling the wastestream transferred to the sorbent treatment area (20) until sufficient time has passed to substantially absorb the target element or isotope forming a part of the wastestream, wherein said at least one sorbent substance is selected from a group consisting of powdered, granular, liquid ionic flocculent and other forms of sorbents;

communicating the wastestream from the area (20) to a means for separation and settling (33), wherein at least a portion of the wastestream is separated out to a solid material, and wherein, between the sorbent treatment area (20) and the means for separation and settling (33) communicating a first means (22A, 38), for selectable recycle to the treatment area (20), when selected, of a portion of the wastestream chosen not to pass through the means for separation and settling (33); and

transferring the solid material from the separation and settling means (33) to the collection tank (28), and transferring the remaining wastestream from the means (33) to a filter unit (34), and wherein, between the separation and settling means (33) and the filter unit (34) communicating a second means (31A, 38) for selectable recycle to the treatment area (20), when selected, of a portion of the wastestream chosen not to pass through the filter unit (34).

40. The system of claim 39, wherein as a part of step (II), one sorbent material is added and mixed (24, 24a) in the sorbent treatment area (20), and the first means (22A, 38) for selectable recycle to the treatment area (20) being selected and repeated when necessary until sufficient time has passed to substantially absorb the at least one subject target element.

41. The system of claim 39, wherein as a part of step (II), the second means (31A, 38) for selectable recycle being utilized for removal of sorbents and other solids without passing such materials through the filter unit (34), and being utilized when a sorbent currently being used is required to be removed prior to a subsequent sorbent being added to the sorbent treatment area (20).

42. The system of claim 39, wherein, step (III) is a Solid-Liquid Separation step further comprising the substeps of:

filtering the remaining wastestream through a filter media (35) of the filter unit (34),

communicating with a rejected side of the filter media (35) a third means (36A, 38) for selectable recycle to the treatment area (20), for recycling at least a part of the wastestream, not passing through the media (35), to the sorbent treatment area (20), and

contemporaneously directing at least a part of the wastestream, passing through the media (35) to a manifold (41); and

wherein, the wastestream processes through the separation and settling device (33) and to the filter unit (34) and wherein a reject portion from the reject side of the filter media (35) of the filter unit (34) being returned through the third means (36A, 38) for selectable recycle to the treatment area (20) for further processing.

43. The system of claim 42, wherein, when no solids are present in the wastestream and no need to remove solids prior to passage through sorbent treatment area (20), and only one sorbent is utilized in the sorbent treatment area (20), the first means for selectable recycle (22A, 38) and the third means for selectable recycle (36A, 38), to the treatment area (20) being utilized.

44. The system of claim 42, wherein, when at least two separate processing passes through the sorbent treatment area (20) are selected and utilized or a first sorbent is removed from the treatment area (20) before adding and using a second or respective additional sorbent, for absorption of targeted element substances, then the second means for selectable recycle (31A, 38), to the treatment area (20) being utilized.

45. The system of claim 42 wherein, adding one and more than one sorbents to the sorbent treatment area (20) in a manner selected to address sorbency-targeting of one and more than one of said subject target element or isotope, and such that said adding of respective individual sorbents when chosen creates a sequential adding of sorbents and sorbent addition strategy to best absorb the subject target element in the treatment area (20), and when present more than one such subject target element, during related or contemporaneous time periods while the subject target element of interest is present in the treatment area (20).

46. The system of claim 42, wherein, step (IV) is an Adjustable and Configurable Ion exchange (IX) step further comprising:

processing the wastestream passing into the manifold system (41) by selective removal of isotopes, wherein the system (41) comprises at least one vessel unit (42) for ion exchange, the unit (42) being served and connected to at least one manifold line (43), and wherein one and more such vessels are selectively deployable in series, and adjustable and configurable through bypass function, in determining flow path and selective IX treatment through the system (41), and

exiting the remaining wastestream from the system (41) to a means of IX effluent conveyance (51).

47. The system of claim 46, wherein, as a part of said step (V), the substeps comprise:

conveying the remaining wastestream on the conveyance (51) to a means for storing and monitoring fluid (50),

passing at least a portion of the remaining wastestream from the means (50) to at least one of the group consisting of;

the Water Discharge (Va), and the Drying of resulting wastestream dissolved solids (Vb); and

contemporaneously guiding at least a part of the remaining wastestream through a recycling subprocess where the wastestream is returned to the means for storing and monitoring fluid (50);

wherein;

the Water Discharge (Va) comprises at least a means for discharging the remaining wastestream as clean water to the environment; and

the Drying (Vb) comprises at least a means for providing evaporator feed conveyance (53) of at least a part of the remaining wastestream from the means (50), a means for evaporation (54) in communication with the means (53), and a means connected to the evaporation (54) for selective recycle back to the facility or storage area (6).

48. The system of claim 47, wherein:

the recycling subprocess comprises at least;

a means (50R) for communicating and transferring the at least part of the remaining wastestream from the means for storing and monitoring fluid (50) to the means of IX effluent conveyance (51),

means for providing pH adjustment in communication with the means of conveyance (51), and

means of measuring pH, in communication with the conveyance (51), before the wastestream is transferred to the IX effluent conveyance (51) and returned to the means for storing and monitoring fluid (50).

51. The system in accordance with claim 32, wherein, the system further being provided with means for separating and settling solids when present in the aqueous wastestream prior to step (I), and between step (II) and step (III), and communicating the solids separated to a solids collection tank (28).

49. A system for treating a liquid or aqueous wastestream, when internally enclosed within a treatment environment substantially eliminating foam generated during processing, the wastestream consisting of at least one of a group of wastes consisting of radioactive concentrate fluid, historic waste and other forms of environmental or hazardous waste or radwaste product from a nuclear facility;

inherently containing, without specific addition to said system, chelant and organics; and

converting the wastestream into at least one of two selected forms including a form which can be evaporated to a solid, or solidified form, which can be safely discharged to an industrial or plant facility, and an aqueous form which can be safely discharged to the environment, said system comprising the steps of;

(I) ozone oxidizing the wastestream through a factor of pH adjustment and temperature mediated ozonation such that any existing said chelant and organics thereof are substantially rendered non-effective as a chelant of metals or destroyed, whereby pH is lowered and rendered substantially unchanging and CO2 is produced, and the wastestream is rendered subject to or permissive of, by virtue of the absence of any existing binding chelant, treatment by the following steps (II), (III), (IV) and (V);

a temperature range of the ozone oxidizing being in a range of from about 55 degrees F. or about 13 degrees Centigrade to less than or equal to about 80 degrees F. or about 27 degrees Centigrade;

(II) mixing the wastestream with at least one target Sorbent material for Isotopic Reduction;

(III) separating the wastestream into Solid and Liquid components;

(IV) treating the wastestream by Selective Ion exchange (IX); and

(V) final processing, wherein at least one step is chosen from group consisting of;

(Va) discharging the wastestream in said aqueous form, and

(Vb) drying of a resulting wastestream having dissolved solids to Dry Solids, as said solidified form;

wherein, the process is subject to control through substantially eliminating foam generated during processing; and

, wherein, further including adding an anti-foaming agent to the recycle oxidation vessel (12) in Step (I).

52. The system in accordance with claim 49, wherein, the temperature in step (I) being maintained through adjustment in a range of from about 20 degrees C. to about 25 degrees C.;

pH in step (I) is maintained through adjustment in a range of from about 11 to about 12; and

, wherein, the ORP is in a range of from about +500 mV to about +1000 mV, for indication that chelant oxidation processing is occurring;

wherein, said step (II) of the system further comprising means for sequentially and selectively recycling the aqueous wastestream through multiple recycle lines such that one and multiple sorbent materials can be added to a sorbent container (20) to target existing radioisotopes when present; and

wherein, the system further being provided with means for separating and settling solids when present in the aqueous wastestream prior to step (I), and between step (II) and step (III), and communicating the solids separated to a solids collection tank (28).

50. A system for treating a liquid or aqueous wastestream, the wastestream comprising at least one of a group of wastes consisting of radioactive concentrate fluid, historic waste and other forms of environmental or hazardous waste or radwaste product from a nuclear facility;

inherently containing when present, without specific addition to said system, chelant and organics; and

converting the wastestream into at least one of two selected forms including a form which can be evaporated to a solid, or solidified form, which can be safely discharged to an industrial or plant facility, and an aqueous form which can be safely discharged to the environment, said system comprising the steps of;

(I) ozone oxidizing the wastestream using a recycle oxidation vessel (12) having incoming and outgoing lines and a recirculation loop, through a factor of pH adjustment and temperature mediated ozonation such that any existing said chelant and organics thereof, are substantially rendered non-effective as a chelant of metals or destroyed, whereby pH is lowered and rendered substantially unchanging and a CO2 gas is produced, and the wastestream is rendered subject to or permissive of, by virtue of the absence of binding chelant, treatment of cobalt and other metals and other isotopes by following steps (II), (III), (IV) and (V), a temperature range of the ozone oxidizing being in a range of from about 55 degrees F. to less than or equal to about 80 degrees F.;

(II) mixing the wastestream with at least one target Sorbent material for Isotopic Reduction;

(III) separating the wastestream into Solid and Liquid components;

(IV) treating the wastestream by Selective Ion exchange (IX); and

(V) final processing, wherein at least one step is chosen from group consisting of;

(Va) discharging the wastestream in said aqueous form, and

(Vb) drying of a resulting wastestream having dissolved solids to Dry Solids, as said solidified form, the drying being done in an environment where the pH is from about 12 to about 13; and

wherein, an antifoaming agent being used for decreasing the presence of a foam volume in the presence of, and generated by, the gas during the use of the loop for recirculation of the wastestream to the oxidation vessel (12), and for prevention of foam overflow from said vessel (12).

53. The system in accordance with claim 50;

wherein, the temperature in step (I) being maintained through adjustment in a range of from about 20 degrees C. to about 25 degrees C.;

pH in step (I) is maintained through adjustment in a range of from about 11 to about 12; and

, wherein, the ORP is in a range of from about +500 mV to about +1000 mV, for indication that chelant oxidation processing is occurring;

wherein, said step (II) of the system further comprising means for sequentially and selectively recycling the aqueous wastestream through multiple recycle lines such that one and multiple sorbent materials can be added to a sorbent container (20) to target existing radioisotopes when present; and

the system further being provided with means for separating and settling solids when present in the aqueous wastestream prior to step (I), and between step (II) and step (III), and communicating the solids separated to a solids collection tank (28).

54. A system for treating a liquid or aqueous wastestream comprising at least one of a group of wastes consisting of radioactive concentrate fluid, historic waste and other forms of environmental or hazardous waste or radwaste product from a nuclear facility;

inherently containing when present, without specific addition, chelant and organics; and

converting the wastestream into at least one of two selected forms including a form which can be solidified, or solidified form, for safe disposal and an aqueous form which can be safely discharged to the environment, the system comprising the steps of;

ozone oxidizing the wastestream where a temperature is maintained through adjustment in a range of from about 20 degrees C. to about 25 degrees C., a pH is maintained through adjustment in a range of from about 11 to about 12, and, wherein, an ORP in a range of from about +500 mV to about +1000 mV indicates that chelant oxidation processing and chelant destruction is occurring, and wherein the ozone oxidizing is adjusted through treatment with anti-foaming substances;

such that any existing chelant chemical compound or organic substance contained in the wastestream is substantially rendered non-effective as a chelant of metals or destroyed thereby releasing the metals into ionic form for treatment as follows,

mixing the wastestream with at least one target Sorbent material for Isotopic Reduction;

separating the wastestream into Solid and Liquid components; and

final processing, wherein at least one step is chosen from a group consisting of;

discharging the wastestream in said aqueous form, and

drying of a resulting wastestream having dissolved solids to Dry Solids, as said solidified form.