Concentrate treatment system

• US 9,283,418 B2
• Filed: 05/23/2013
• Issued: 03/15/2016
• Est. Priority Date: 10/15/2010
• Status: Active Grant

• Current Assignee: AVANTech, LLC
• Original Assignee: Avantech
• Inventors: Brunsell, Dennis A., Jensen, Charles E., Beets, Larry E.
• Primary Examiner(s): Nguyen, Nam
• Assistant Examiner(s): GURTOWSKI, RICHARD C
• Application Number:
  US13/900,548
• Publication Number:
  US 20150380117A1
• Time in Patent Office: 1,027 Days
• Field of Search: None
• US Class Current: 1/1
• CPC Class Codes: A62D 3/00 Processes for making harmful chemical substances harmless or less harmful, by effecting a chemical change in the substances consuming noxious gases by combustion F23G7/06
• CPC Class Codes: A62D 3/30 by reacting with chemical agents
• CPC Class Codes: A62D 3/32 by treatment in molten chemical reagent, e.g. salts or metals
• CPC Class Codes: A62D 3/38 by oxidation; by combustion
• CPC Class Codes: C02F 1/001 Processes for the treatment of water whereby the filtration technique is of importance C02F1/44 takes precedence; construction of filters in general B01D24/00 - B01D41/00
• CPC Class Codes: C02F 1/20 by degassing, i.e. liberation of dissolved gases degasification of liquids in general B01D19/00; arrangement of degassing apparatus in boiler feed supply F22D
• 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 1/72 by oxidation C02F1/4672 takes precedence
• CPC Class Codes: C02F 1/78 with ozone C02F1/4672 takes precedence
• CPC Class Codes: C02F 2101/006 Radioactive compounds
• CPC Class Codes: C02F 2103/34 from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
• CPC Class Codes: C02F 2209/001 Upstream control, i.e. monitoring for predictive control
• CPC Class Codes: C02F 2209/006 comprising a software program or a logic diagram
• 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 2301/046 Recirculation with an external loop
• CPC Class Codes: C02F 9/00 Multistage treatment of water, waste water or sewage
• CPC Class Codes: G21F 9/04 Treating liquids
• 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: G21F 9/28 : Treating solids
• CPC Class Codes: G21F 9/30 : Processing separating different isotopes of the same chemical element B01D59/00

Abstract

One aspect of the invention provides a system for treating wastestream, particularly a liquid or aqueous 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. Another aspect 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) to inactivate or destroy existing chelants, Solid-Liquid separation (III), and Selective Ion Exchange (IV) to deliver the wastestream to final processing. Still further aspects of the invention address the recovery and safe handling of substances such as C-14.

Claims

1. A process for treating a liquid or aqueous wastestream consisting 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 is a solidified form for safe disposal and an aqueous form, which can be safely discharged to the environment, said process comprising the steps, designated as Roman numerals;

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

(I) oxidizing the wastestream via addition of an oxidant to the wastestream such that any existing chelant material or substance contained in the wastestream is 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 isotopes for removal;

(II) mixing the wastestream with at least one target Sorbent material such that isotopes are removed from the wastestream;

(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;

wherein, step (I) is an Oxidation or Ozone Oxidation step, further comprising the substeps of;

communicating the wastestream from a stored location through a first hydrocyclone, whereat a solids partition of the wastestream is conveyed to a solids collection tank, and a remaining part of the wastestream is conveyed to a recycle oxidation vessel for processing therein,

conveying the wastestream after processing in the recycle oxidation vessel to a pH and temperature measurement area and ORP measurement station, and

transferring at least part of the wastestream to a heat exchanger, the heat exchanger communicating with an eductor supply feed and an ozone eductor and mixing equipment through which the wastestream is communicated to an oxidation return line back in recycle to the recycle oxidation vessel, said oxidation return line further communicating with and being contemporaneously served by a chemical injector;

wherein, step (II) is a Sorption or Powder Sorbent isotope removal step, further comprising the substeps of;

marshaling at least a part of the remaining wastestream not being transferred to the heat exchanger, and transferring the remaining wastestream to a sorbent treatment area,

selecting at least one sorbent substance to remove at least one subject target element or isotope forming a part of the wastestream transferred to the sorbent treatment area, adding the at least one sorbent substance selected to the sorbent treatment area 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 absorb the target element or isotope forming a part of the wastestream, and recycling the wastestream transferred to the sorbent treatment until sufficient time has passed to 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, or liquid ionic flocculent and other forms of sorbents;

communicating the wastestream from the sorbent treatment area to a second hydrocyclone. wherein at least a portion of the wastestream is separated out to a solid material, and wherein, between the sorbent treatment area and the second hydrocyclone communicating a first recycle line to the sorbent treatment area, when selected, of a portion of the wastestream chosen not to pass through the second hydrocyclone,

transferring the solid material from the second hydrocyclone to the solids collection tank, and transferring the remaining wastestream from the second hydrocyclone to a filter unit, and wherein, between the second hydrocyclone and the filter unit communicating a second recycle line to the sorbent treatment area, when selected, of a portion of the wastestream chosen not to pass through the filter unit.

2. The process of claim 1, wherein, as a part of step (I) the wastestream is conveyed or transferred from a stored location to a recycle oxidation vessel;

and

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, said recycle oxidation vessel being selectively served by a heat exchanger when required to adjust the temperature to a more favorable oxidation range; and

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

3. The process of claim 2, wherein the pH of the wastestream is determined and adjustment performed using a chemical injector.

4. The process of claim 2, wherein, an antifoaming agent is utilized, said agent being provided through the chemical injector.

5. The process of claim 3, wherein, the pH is below about 12.5.

6. The process of claim 4, wherein an ORP of the wastestream is from about +300 mV to about +1000 mV after adjustment for the pH.

7. The process of claim 2, wherein the heat exchanger operates to lower the temperature of the wastestream to a temperature of less than about 80 degrees F. or about 27 degrees C.

8. The process of claim 2, wherein the heat exchanger operates to lower the temperature of the wastestream to a temperature of less than or equal to about 60 degrees F. or about 16 degrees C.

23. The process according to claims 1, 9, or 22,

wherein, the wastestream contains C-14;

and

wherein, in step (II), further comprising adding as a part of the mixing at least one substance selected from a group of substances consisting of a) CaCl2, b) Ca(NO3)2 and c) other soluble calcium salts.

24. The process according to claims 1, 9 or 22,

wherein, the wastestream contains C-14, and further comprising:

prior to step (I), lowering the wastestream to a pH range of about 5 to about 7, and rendering the treatment environment such that it can be evacuated at a vacuum up to about 28 in. Hg.; and

returning the pH to a level to reconvert a boric acid volume to a sodium borate volume so that any dissolved boric acid/sodium borate is not removed in step (I).

25. The process according to claims 1, 9, or 22, wherein, the wastestream contains C-14;

and further comprising;

after step (I), lowering the pH of the wastestream to a pH range of about 5 to about 7, and rendering the treatment environment such that it can be evacuated at a vacuum up to about 28 in. Hg.; and

returning the pH to a level to reconvert a boric acid volume to a sodium borate volume so that any dissolved boric acid/sodium borate is not removed in step (II).

26. The process according to claims 1, 9, or 22, wherein, the wastestream contains C-14;

and further comprising;

after step (I), lowering the pH of the wastestream to a pH range of about 5 to about 7, and rendering the treatment environment such that it can be evacuated through a degassifier with vacuum; and

returning the pH to a level to reconvert a boric acid volume to a sodium borate volume so that any dissolved boric acid/sodium borate is not removed in step (I).

27. The process according to claims 1, 9 or 22, wherein, the wastestream contains C-14;

and further comprising;

after step (I), lowering the pH of the wastestream to a pH range of about 5 to about 7, and rendering the treatment environment such that it can be evacuated through a degassifier with vacuum; and

returning the pH to a level to reconvert a boric acid volume to a sodium borate volume so that any dissolved boric acid/sodium borate is not removed in step (II).

28. The process according to claims 1, 9 or 22,

wherein, just prior to the final processing step (V), placing the resulting wastestream in a monitor tank where the wastestream can be analyzed for isotopic content.

29. The process according to claim 1, 9 or 28,

wherein, in the drying step (Vb) the wastestream is brought to a temperature range of greater than or equal to about 100 degrees C. to a temperature of less than or equal to about 240 degrees C.

9. A process 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 consisting of a form which is evaporated to a 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 process comprising the steps, designated as Roman numerals;

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

(I) oxidizing the wastestream via addition of an oxidant to the wastestream such that any existing chelant material, or substance contained in the wastestream is 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 isotopes for removal or ion exchange;

(II) mixing the wastestream with at least one target Sorbent material such that isotopes are removed from the wastestream;

(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;

wherein, step (I) is an Oxidation or Ozone Oxidation step, further comprising the substeps of;

communicating the wastestream from a stored location through a first hydrocyclone, whereat a solids partition of the wastestream is conveyed to a solids collection tank, and a remaining part of the wastestream is conveyed to a recycle oxidation vessel for processing therein,

conveying the wastestream after processing in the recycle oxidation vessel to a pH and temperature measurement area and ORP measurement station, and

transferring at least part of the wastestream to a heat exchanger, the heat exchanger communicating with an eductor supply feed and an ozone eductor and mixing equipment through which the wastestream is communicated to an oxidation return line back in recycle to the recycle oxidation vessel, said oxidation return line further communicating with and being contemporaneously served by a chemical injector;

wherein, step (II) is a Sorption or Powder Sorbent isotope removal step, further comprising the substeps of;

marshaling at least a part of the remaining wastestream not being transferred to the heat exchanger, and transferring the remaining wastestream to a sorbent treatment area,

selecting at least one sorbent substance to remove at least one subject target element or isotope forming a part of the wastestream transferred lo the sorbent treatment area, adding the at least one sorbent substance selected to the sorbent treatment area 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 absorb the target element or isotope forming a part of the wastestream, and recycling the wastestream transferred to the sorbent treatment area until sufficient time has passed to 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, or liquid ionic flocculent and other forms of sorbents;

communicating the wastestream from the sorbent treatment area to a second hydrocyclone, wherein at least a portion of the wastestream is separated out to a solid material and wherein, between the sorbent treatment area and the second hydrocyclone communicating a first recycle line to the sorbent treatment area, when selected, of a portion of the wastestream chosen not to pass through the second hydrocyclone,

transferring the solid material from the second hydrocyclone to the solids collection tank, and transferring the remaining wastestream from the second hydrocyclone to a filter unit, and wherein, between the second hydrocyclone and the filter unit communicating a second recycle line to the sorbent treatment area, when selected, of a portion of the wastestream chosen not to pass through the filter unit.

10. The process of claim 9, wherein as a part of step (II), one sorbent material is added and mixed in the sorbent treatment area, and the first recycle line to the sorbent treatment area being selected and repeated until sufficient time has passed to absorb the at least one target element or isotope.

11. The process of claim 9, wherein as a part of step (II), the second recycle line being utilized for removal of sorbents and other solids without passing such materials through the filter unit, 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.

12. The process of claim 9, wherein, step (III) is a Solid-Liquid Separation step further comprising the substeps of:

filtering the remaining wastestream through a filter media of the filter unit, communicating with a rejected side of the filter media a third recycle line to the sorbent treatment area, for recycling at least a part of the wastestream, not passing through the filter media, to the sorbent treatment area, and

contemporaneously directing at least a part of the wastestream, passing through the filter media to a manifold system.

13. The process of claim 12, wherein the wastestream processes through the second hydrocyclone and to the filter unit, and wherein a reject portion from the reject side of the filter media of the filter unit being returned through the third recycle line to the sorbent treatment area for further processing.

14. The process of claim 12, wherein, when no solids are present in the wastestream and there is no need to remove solids prior to passage through sorbent treatment area, and only one sorbent is utilized in the sorbent treatment area, the first recycle line and the third recycle line to the sorbent treatment area are utilized.

15. The process of claim 12, wherein, when at least two separate processing passes of the wastestream through the sorbent treatment area are selected and utilized or a first sorbent is removed from the sorbent treatment area before adding and using a second or respective additional sorbent for absorption of target elements or isotopes, then the second recycle line to the sorbent treatment area is utilized.

16. The process of claim 12, wherein, adding at least one sorbent to the sorbent treatment area in a manner selected to address sorbency-targeting of at least one target element or isotope such that said adding of respective individual sorbents when chosen creates a sequential adding of sorbents and sorbent addition strategy to best absorb the target element or isotope in the sorbent treatment area during related or contemporaneous time periods while the target element or isotope is present in the sorbent treatment area.

17. The process of claim 12, wherein, step (IV) is an Adjustable and Configurable Ion exchange (IX) step further comprising:

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

exiting the remaining wastestream from the manifold system to an IX effluent line.

18. The process of claim 17, wherein, as a part of said step (V), the substeps comprise:

conveying the remaining wastestream on the IX effluent line to a monitor tank,

passing at least a portion of the remaining wastestream from the monitor tank to at least one of the group consisting of;

the Wastestream 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 monitor tank.

19. The process of claim 18, wherein:

the Wastestream Discharge (Va) comprises at least a discharge line, said discharge line discharging the remaining wastestream as clean water to the environment; and

the Drying of resulting wastestream dissolved solids (Vb) comprises at least an evaporator feed line of at least a part of the remaining wastestream from the monitor tank, an evaporator unit in communication with the evaporator feed line, and a line connected to the evaporator unit for selective recycle back to the stored location.

20. The process of claim 19, wherein:

the recycling subprocess comprises at least;

a monitor tank recycle line for communicating and transferring the at least part of the remaining wastestream from the monitor tank to the IX effluent line,

a chemical injector in communication with the IX effluent line, and a pH measurement area in communication with the IX effluent line, before the wastestream is transferred to the IX effluent line and returned to the monitor tank.

21. The process of claim 12, wherein the process is coordinated and controlled as to each process step by a process logic controller.

22. A process 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 is evaporated to a 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 process comprising the steps of;

(I) oxidizing the wastestream through a factor of pH adjustment such that any existing chelant material, or substance thereof, is rendered non-effective as a chelant of metals or destroyed, whereby pH is lowered and rendered 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 isotopes for removal or ion exchange;

(II) mixing the wastestream with at least one target Sorbent material such that isotopes are removed from the wastestream;

(III) separating the wastestream into Solid or 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;

wherein, step (I) is an Oxidation or Ozone Oxidation step, further comprising the substeps of;

communicating the wastestream from a stored location through a first hydrocyclone, whereat a solids partition of the wastestream is conveyed to a solids collection tank, and a remaining part of the wastestream is conveyed to a recycle oxidation vessel for processing therein,

conveying the wastestream after processing in the recycle oxidation vessel to a pH and temperature measurement area and ORP measurement station, and

transferring at least part of the wastestream to a heat exchanger, the heat exchanger communicating with an eductor supply feed and an ozone eductor and mixing equipment through with the wastestream is communicated to an oxidation return line back in recycle to the recycle oxidation vessel, said oxidation return line further communicating with and being contemporaneously served by a chemical injector;

wherein, step (II) is a Sorption or Powder Sorbent isotope removal step, further comprising the substeps of;

marshaling at least a part of the remaining wastestream not being transferred to the heat exchanger, and transferring the remaining wastestream to a sorbent treatment area,

selecting at least one sorbent substance to remove at least one subject target element or isotope forming a part of the wastestream transferred to the sorbent treatment area, adding the at least one sorbent substance selected to the sorbent treatment area 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 absorb the target element or isotope forming a part of the wastestream, and recycling the wastestream transferred to the sorbent treatment until sufficient time has passed to 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, or liquid ionic flocculent and other forms of sorbents;

communicating the wastestream from the sorbent treatment area to a second hydrocyclone, wherein at least a portion of the wastestream is separated out to a solid material, and wherein, between the sorbent Treatment area and the second hydrocyclone communicating a first recycle line to the sorbent treatment area, when selected, of a portion of the wastestream chosen not to pass through the second hydrocyclone,

transferring the solid material from the second hydrocyclone to the solids collection tank, and transferring the remaining wastestream from the second hydrocyclone to a filter unit, and wherein, between the second hydrocyclone and the filter unit communicating a second recycle line to the sorbent treatment area, when selected, of a portion of the wastestream chosen not to pass through the filter unit.

30. A process 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 is a solidified form for safe disposal and an aqueous form which can be safely discharged to the environment, the process 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 about 18.3 degrees C., such that any existing chelant chemical compound or organic substance contained in the wastestream is rendered non-effective as a chelant of metals or destroyed thereby releasing the metals into ionic form for treatment in the process with the steps II, III, IV and V;

(II) mixing the wastestream with at least one target Sorbent material such that isotopes are removed from the wastestream;

(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; and

wherein at least one substep is chosen from a group, when the wastestream contains C-14, consisting of;

in step (II), further comprising adding as a part of the mixing at least one substance selected from a group of substances consisting of a) CaCl2, b) Ca(NO3)2 and c) other soluble calcium salts,

prior to step (I), lowering the pH of the wastestream to a pH range of about 5 to about 7, and rendering a wastestream processing environment such that it can be evacuated at a vacuum up to about 28 in. Hg., and returning the pH to a level to reconvert a boric acid volume in the wastestream to a sodium borate volume, so that any dissolved boric acid/sodium borate is not removed in step (II),

after step (I), lowering the pH of the wastestream to a pH range of about 5 to about 7, and rendering a wastestream processing environment such that it can be evacuated at a vacuum up to about 28 in. Hg,; and

returning the pH to a level to reconvert a boric acid volume in the wastestream to a sodium borate volume, so that any dissolved boric acid/sodium borate is not removed in step (II),

prior to step (I), lowering the pH of the wastestream to a pH range of about 5 to about 7, and rendering a wastestream processing environment such that it can be evacuated through a degassifier with vacuum; and

returning the pH to a level to reconvert a boric acid volume in the wastestream to a sodium borate volume, so that any dissolved boric acid/sodium borate is not removed in step (I),

after step (I), lowering the pH of the wastestream to a pH range of about 5 to about 7, and rendering a wastestream processing environment such that it can be evacuated through a degassifier with vacuum; and

returning the pH to a level to reconvert to a boric acid volume in the wastestream to a sodium borate volume, so that any dissolved boric acid/sodium borate is not removed in step (II),

just prior to the final processing step (V), placing the resulting wastestream in a monitoring tank where the wastestream can be analyzed for isotopic content, and

in the drying step (Vb) the wastestream is brought to a temperature range of greater than or equal to about 100 degrees C. to a temperature of less than or equal to about 240 degrees C.; and

wherein, chelant and organics when present, being one or more of a group consisting of EDTA, citric acid, LOMI solution, and other chelants.

31. A process 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 process, chelant and organics; and

converting the wastestream into at least one of two selected forms including a form which is evaporated to a solidified form which can be safely discharged to an industry or plant facility, and an aqueous form which can be safely discharged to the environment, said process 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 rendered non-effective as a chelant of metals or destroyed, whereby pH of the wastestream is lowered and rendered 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 C. to less than or equal to about 80 degrees F. or about 27 degrees C.;

(II) mixing the wastestream with at least one target Sorbent material such that isotopes are removed from the wastestream;

(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 at least one substep is chosen from a group, when the wastestream contains C-14, consisting of;

the process being subject to control through eliminating foam generated during processing; and

, wherein, further including adding an anti-foaming agent to a recycle oxidation vessel in step (I),

in step (II), further comprising adding as a part of the mixing at least one substance selected from a group of substances consisting of a) CaCl2, b) Ca(NO3)2 and c) other soluble calcium salts,

prior to step (I), lowering the pH of the wastestream to a pH range of about 5 to about 7, and rendering a wastestream processing environment such that it can be evacuated at a vacuum up to about 28 in. Hg., and returning the pH to a level to reconvert a boric acid volume in the wastestream to a sodium borate volume, so that any dissolved boric acid/sodium borate is not removed in step (I),

after step (I), lowering the pH of the wastestream to a pH range of about 5 to about 7, and rendering a wastestream processing environment such that it can be evacuated at a vacuum up to about 28 in. Hg.; and

returning the pH to a level to reconvert a boric acid volume in the wastestream to a sodium borate volume, so that any dissolved boric acid/sodium borate is not removed in step (II),

prior to step (I), lowering the pH of the wastestream to a pH range of about 5 to about 7, and rendering a wastestream processing environment such that it can be evacuated through a degassifier with vacuum; and

returning the pH to a level to reconvert a boric acid volume in the wastestream to a sodium borate volume, so that any dissolved boric acid/sodium borate is not removed in step (I),

after step (I), lowering the pH of the wastestream to a pH range of about 5 to about 7, and rendering a wastestream processing environment such that it can be evacuated through a degassifier with vacuum; and

returning the pH to a level to reconvert a boric acid volume in the wastestream to a sodium borate volume, so that any dissolved boric acid/sodium borate is not removed in step (II),

just prior to the final processing step (V), placing the resulting wastestream in a monitor tank where the wastestream can be analyzed for isotopic content, and in the drying step (Vb) the wastestream being brought to a temperature range of greater than or equal to about 100 degrees C. to a temperature of less than or equal to about 240 degrees C.

32. A process 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 process, chelant and organics; and

converting the wastestream into at least one of two selected forms including a form which is evaporated to a 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 process comprising the steps of;

(I) ozone oxidizing the wastestream using a recycle oxidation vessel 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 rendered non-effective as a chelant of metals or destroyed, whereby pH is lowered and rendered unchanging and a CO2 gas is produced, and the wastestream is rendered subject to or permissive of, by virtue of an absence of binding chelant, treatment of cobalt and other metals isotopes by following steps (II), (III), (IV) and (V), a temperature range of the ozone oxidizing being m 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 such that isotopes are removed from the wastestream;

(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 at least one substep is chosen from a group, when the wastestream contains C-14, consisting of;

an antifoaming agent being used for decreasing a presence of a foam volume in the presence of, and generated by, a gas during the use of the loop for recirculation of the recycle oxidation vessel, the process being subject to control through eliminating foam generated during processing; and

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

in step (II), further comprising adding as a part of the mixing at least one substance selected from a group of substances consisting of a) CaCl2, b) Ca(NO3)2 and c) other soluble calcium salts,

prior to step (I), lowering the pH of the wastestream to a pH range of about 5 to about 7, and rendering a wastestream processing environment such that it can be evacuated at a vacuum up to about 28 in. Hg., and returning the pH to a level to reconvert a boric acid volume in the wastestream to a sodium borate volume, so that any dissolved boric acid/sodium borate is not removed in step (I),

after step (I), lowering the pH of the wastestream to a pH range of about 5 to about 7, and rendering a wastestream processing environment such that it can be evacuated at a vacuum up to about 28 in. Hg.; and

returning the pH to a level to reconvert a boric acid volume in the wastestream to a sodium borate volume, so that any dissolved boric acid/sodium borate is not removed in step (II),

prior to step (I), lowering the pH of the wastestream to a pH range of about 5 to about 7, and rendering a wastestream processing environment such that it can be evacuated through a degassifier with vacuum; and

returning the pH to a level to reconvert a boric acid volume in the wastestream to a sodium borate volume, so that any dissolved boric acid/sodium borate is not removed in step (I),

after step (I), lowering the pH of the wastestream to a pH range of about 5 to about 7, and rendering a wastestream processing environment such that it can be evacuated through a degassifier with vacuum; and

returning the pH to a level to reconvert a boric acid volume in the wastestream to a sodium borate volume, so that any dissolved boric acid/sodium borate is not removed in the following step (II), just prior to the final processing step (V), placing the resulting wastestream in a monitor tank where the wastestream can be analyzed for isotopic content, and

in the drying step (Vb) the wastestream being brought to a temperature range of greater than or equal to about 100 degrees C. to a temperature of less than or equal to about 240 degrees C.

33. A process 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 is a solidified form for disposal and an aqueous form which can be safely discharged to the environment, the process comprising the steps of;

(I) 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 rendered non-effective as a chelant of metals or destroyed thereby releasing the metals into ionic form for treatment as follows,

(II) mixing the wastestream with at least one target Sorbent material such that isotopes are removed from the wastestream;

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

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

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

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

wherein at least one substep is chosen from a group, when the wastestream contains C-14, consisting of;

in step (II), further comprising adding as a part of the mixing at least one substance selected from a group of substances consisting of a) CaCl2, b) Ca(NO3)2 and c) other soluble calcium salts,

prior to step (I), lowering the pH of the wastestream to a pH range of about 5 to about 7, and rendering a wastestream processing environment such that it can be evacuated at a vacuum up to about 28 in. Hg., and returning the pH to a level to reconvert a boric acid volume in the wastestream to a sodium borate volume, so that any dissolved boric acid/sodium borate is not removed in step (I),

after step (I), lowering the pH of the wastestream to a pH range of about 5 to about 7, and rendering a wastestream processing environment such that it can be evacuated at a vacuum up to about 28 in. Hg.; and

returning the pH to a level to reconvert a boric acid volume in the wastestream to a sodium borate volume, so that any dissolved boric acid/sodium borate is not removed in the following step (II),

prior to step (I), lowering the pH of the wastestream to a pH range of about 5 to about 7, and rendering a wastestream processing environment such that it can be evacuated through a degassifier with vacuum; and

returning the pH to a level to reconvert a boric acid volume in the wastestream to a sodium borate volume, so that any dissolved boric acid/sodium borate is not removed in step (I),

after step (I), lowering the pH of the wastestream to a pH range of about 5 to about 7, and rendering a wastestream processing environment such that it can be evacuated through a degassifier with vacuum; and

returning the pH to a level to reconvert a boric acid volume in the wastestream to a sodium borate volume, so that any dissolved boric acid/sodium borate is not removed in step (II),

just prior to the final processing step (IV), placing the resulting wastestream in a monitor tank where the wastestream can be analyzed for isotopic content, and

in the drying step (IVb) the wastestream being brought to a temperature range of greater than or equal to about 100 degrees C. to a temperature of less than or equal to about 240 degrees C.