WO1991013030A1

WO1991013030A1 - Processing mixed waste

Info

Publication number: WO1991013030A1
Application number: PCT/US1991/001036
Authority: WO
Inventors: Brian D. Metz
Original assignee: Southern California Edison Company
Priority date: 1990-02-21
Filing date: 1991-02-15
Publication date: 1991-09-05
Also published as: US5076936A

Abstract

Removing radioactive contaminants from liquid hazardous material such as oil includes recirculating the material between a processing tank (11) and a filter medium (18). The material is heated (15) to increase viscosity during the circulation through the tank (11) and filters (18). Chemicals including chelating agents are added to enhance the removal of the radioactive elements. Water is added to the processing tank (15) or upstream, in a settling tank (31), to effect a water wash of the liquid hazardous material. A pre-filter (35) stage upstream of the settling tank (31) is followed by a mid-range filter stage (18) in the recirculation loop with the main processing tank (11). A finishing filter stage (24, 25) is in the outlet from the main processing tank.

Description

PROCESSING MIXED WASTE

BACKGROUND

The disposal of hazardous waste containing radioactive elements is expensive and difficult. At the same time, it is important to safeguard the environment.

This invention relates to the processing of mixed waste. In particular, the invention relates to the removal of radioactivity from liquid hazardous waste which also includes material known as mixed waste. Moreover, the treatment should be considered to effect treatment of solid hazardous waste. Such treatment would include a step to liquify the waste so that the treatment is then effected on a liquid hazardous waste. As such, the term "liquid hazardous waste" is to be considered to include liquid hazardous waste and materials which are no longer useable and also other waste such as solid waste which is liquified. Liquid hazardous waste also refers to waste oils. The terms "liquid hazardous material" and "liquid hazardous waste" are used interchangeably.

Nuclear electric generating facilities accumulate large volumes of liquid hazardous wastes during normal operation and during maintenance activities. Some of these liquid hazardous wastes are found to be contaminated with radioactive material. Much of the radioactive material is at a low concentration.

Materials such as waste oils and other hazardous or toxic wastes are otherwise known as liquid hazardous waste and it is important to be able to dispose of this material safely and economically. In the United States, this type of waste is governed by the Nuclear Regulatory Commission (NRC) and also by the Environmental Protection Agency (EPA) .

Mixed waste may be generated in several other ways, for example, a solvent used by a power plant worker to clean a radioactively contaminated reactor coolant pump. If the solvent is listed by the EPA as hazardous and the pump is slightly radioactive, the solvent would be a mixed waste. The solvent generally poses a greater chemical hazard than radioactive hazard. Three to 10 percent of Low Level Radioactive Waste (LLW) is also considered mixed waste since it contains both radioactive and hazardous contaminants.

Treatment is a critical step in managing mixed waste. Since no offsite treatment or storage facilities are available for mixed waste, generators try, to the extent practicable, to alter their waste to exclusively hazardous waste for which management options are available. Despite such efforts, mixed waste is still generated, containing hazardous constituents that the EPA bans from disposal until a particular treatment standard is met.

It is an object of the present invention to provide a method of treatment for liquid hazardous material and waste within which is included mixed waste. The applicant believes the treatment will minimize difficulties which currently exist.

SUMMARY

According to the invention, decontaminating or removing radioactive elements or contaminants from a hazardous material being in a liquid phase includes a procedure of recirculating material and filtering the material so circulated.

During circulation, heating is effected to increase the viscosity of the material being recirculated. Additionally, chemicals, such as a chelating agent, are added to the recirculating liquid hazardous material to enhance the removal of radioactive elements from the liquid hazardous material.

According to a preferred form of the invention, prior to entry into a processing tank where recirculation, heating and „hemical addition is effected, the liquid hazardous material is subject to a settling step where water is removed from the liquid hazardous material.

Also, in the settling tank step or in the recirculation step through the processing tank, a volume of water is added to the liquid hazardous material to effect a water wash of the liquid hazardous material.

Further, the hazardous material is treated progressively by three different grades of filter, each being progressively finer.

The invention is directed to the method for removal of the radioactive elements, the apparatus for performing such method and the product cleansed of the radioactive elements.

The invention is now further described with reference to the accompanying drawing.

DRAWING

The Figure is a flow diagram illustrating the method and apparatus for performing the invention.

DESCRIPTION

The flow diagram illustrates the mixed waste processing unit for removing radioactive contaminants from liquid hazardous material. The liquid is directed along line 10 to a main processing tank 11. A pump 12 recirculates liquid through the main processing tank as indicated along line 13. Additionally, the pump 12 directs the liquid along line 14 to a heater 15 which returns liquid along line 16 to the main processing tank 11. Pump 12 also directs liquid along line 17 to a recirculating filter 18 which is contained in the line between line 17 and line 13. This filter 18 removes radioactive particulates in the filter medium. Chemicals are added to liquid in the main processing tank 11 through chemical add tank 19 which receives liquid from the pump 12 along line 20. The chemical addition is directed along line 21 back to the main processing tank 11.

An outlet line 22 from pump 12 directs liquid from the main processing tank to a filter bank system 23. Such system 23 includes the finishing filters, or fine filters, for the remaining liquid hazardous material. There are filter elements 24 and 25 in a bank as constituted in the finishing filter 23.

Downstream from the filter bank system 23, the remaining liquid is directed along line 26 to a second chemical addition tank 27 and in turn, a charcoal filter 28. The output from the filter 28 is directed along line 29 to a reservoir or drum 30 for collecting cleaned liquid hazardous material. The liquid can be directed along line 26 and can bypass the chemical addition tank 27 and the charcoal filter 28 can be routed to the main process in tank 11 or to the clean drum 30. This is illustrated by phantom lines 46 and 47, respectively.

Upstream of the main processing tank 11, there is a settling tank 31. The settling tank 31 receives liquid hazardous material from a waste drum 32 which pumps the waste material along line 34 to a pre-filter 35. In turn, the liquid is directed to an outlet line 36 which feeds the settling tank 31. The outlet from the settling tank 31 is directed along line 37 through pump 38. The liquid hazardous material is directed along line 10 while separated water is directed along line 39 or line 40. Water along line 39 is directed to a water separation 41 which acts as an oily waste separator. Oil is returned back for radioactive treatment in the settling tank 31. Along line 40, an ion exchange mixed bed 42 separates the ionic phase of radioactive element and clean liquid is directed along line 43 to the clean drum 30.

In some cases, discharge from the pump 38 can be directed to the second chemical addition tank 27 thereby bypassing the mixed bed 42. This is indicated by phantom line 48. This is for removing radioactive elements in the ionic phase and organics. Alternatively, the mixed bed 42 outlet can be directed to the chemical addition tank 27, as indicated by phantom line 49. This is for removing organics and radioactive elements. Also, in other cases, the settling tank 31 is bypassed and the pre-filter 35 discharges directly with line 10.

The method and apparatus for decontaminating and removing radioactive contaminants from liquid hazardous materials includes the main processing tank 11. The primary hazardous materials treated in the tank are oil (synthetic and otherwise), ethylene glycol, solvents and paints. The radioactive elements or isotopes which are eliminated are Cesium 134, 137, Cobalt 57, 58 and 60, Iodine 131, Chromium 51, Magnesium 54, Niobium 95, Zirconium 95 and Cerium 141, at levels of approximately l.OxlO^"5 to l.OxlO"⁹ micro-curries per cc. The amount of radioactivity are reduced to below detectable levels and the radioactive isotopes are separated from the hazardous or toxic material.

The method and apparatus were geared around the three types of radioactive contaminants: ionic, colloidal, and particulate forms. Different phases of the process removed specific phases or forms of the radioactivity to below detectability. An example of using the apparatus and method of the invention is described below.

The diagram shows the main processing tank 11 and settling tank 31. Flow starts out with liquid hazardous material in the waste drum 32.

The waste drum 32 was initially sampled and categorized. The initial sampling was for types of hazardous material or waste, the types of isotopes and the activity levels of those isotopes.

At this point, each hazardous material was broken down and put into the category for that specific hazardous material. The hazard class was then broken into further categories based on the activity level and the types of isotopes found in that hazardous material. This mixed waste processing unit is generally a batch processing.

Once the categorization and initial sampling had taken place, an amount of about 500 to 800 gallons of hazardous liquid such as oil, solvent, and ethylene glycol are grouped together so that they could be run through this processing unit. For each respective processing, the respective waste drums 32 are pumped into a settling tank 31.

Before the liquid hazardous material was pumped into a settling tank 31, the material was pumped through the pre-filter 35 of 100 microns. The pre-filter 35 is a bag filter. Should the material or waste be relatively clean and there does not appear to be much sediment in the waste, the pre-filter 35 can probably be 50 microns. This eliminates needless radioactive waste as the filters 35, once filled with crud, are disposed of as radioactive in a normal radioactive landfill.

The hazardous material sits in the settling tank for approximately one day to a ^'week depending on the separation of the material. At this point, the material could be identified in several layers. If there were different toxic wastes associated with the initial categorization of the material, these were separated by phases and put back into their correct category or block of wastes. Each specific waste was treated separately at a specific time.

If there was water from the waste, this was run through an ion exchange resin mixed bed 42. The mixed bed can relate to cation only, anion only or a combination of both. This eliminates the ionic phase of the radioactive elements. If this waste were an oilbased waste with no organic contaminants or solvents in the waste, the water could also be run through the oily waste separator 41. The oil can then be run back through the processing stage.

Once the primary type of material was separated and was in the settling tank 31, it was then pumped into the main processing tank 11. In this main processing tank

11, the circulation or recirculation, the heating, and the chemical phases all take place.

Initially, recirculation and heating were the primary steps of the main processing tank. Recirculation is important in relation to the speed of pump 12. A pump

12 at a speed less than 50 gallons per minute occasionally took several days to weeks longer to process the hazardous material. This was due to the fact that the material was not recirculated as fast or as efficiently as a 100-125 gallon per minute pump 12. When treating 500 to 800 gallons of liquid hazardous material, the rate of pump 12 should be greater than 50 gallons per minute. The rate of

125 gallons per minute is effective to obtain the full recirculation of the tank 11.

Heating is important when dealing with a hazardous material, being oil, for the following reasons. Heating changes the viscosity of the oil to allow faster flow rates through filters 18 more efficiently. This permits continuation with the recirculation phase at a higher speed and permits a more thorough mixing.

The recirculation phase is sped up to enhance the separation of the entrained water which is usually within toxic material. Specifically, with oil, there is usually some percentage of water that cannot be removed by normal separation. This is due to the fact that the oil may be emulsified or the water entrained in the oil and thus, cannot be removed. At this point, the heating and the recirculation phase help or enhance removal.

During the recirculation phase, the mixed waste was run through a medium degree of filtration being filter 18. This filter 18 was composed of 50 micron, 10 micron or 1 micron bag filters. The waste was gradually run through all sets of these filters to establish that most of the particulates had been removed by filtering through a 1 micron sized filter. The heater 15 enhanced the ability for the recirculation phase to proceed.

A chemical phase, at this point, was an effective step in the processing of hazardous material, namely, mixed waste. The chemical phase was composed of several chemicals which enhanced or helped remove the radioactive elements.

The first chemical used was a chelating agent, namely, ethylenediaminetetraacetic acid [EDTA] in sodium form. With this, a pH adjuster chemical was added to increase the pH to between 9 and 12 and preferably about 10 or 11. This helps the chelating agent to work more efficiently.

The temperature or heating phase continued to greater than 50° Fahrenheit and preferably until about 175° Fahrenheit to about 190° Fahrenheit was established. Although the higher temperature works more efficiently, the working parts, such as a pump 12, do not usually handle temperatures over 200° Fahrenheit to 220" Fahrenheit.

Several chemicals were selectively added. There were several purposes for the chemicals applied to the process which work and help with the decontamination process. The first was sodium EDTA. The second was sodium hydroxide. The group of chemicals that were carrier chemicals were selectively cesium chloride, cobalt chloride and ferric chloride. Hydrochloric acid, hydrogen peroxide and sodium citrate were then added.

The acid used to neutralize the caustic byproduct was phosphoric or sulfuric. The chloride (cesium chloride, cobalt chloride and ferric chloride) and hydro-chloric acid were added to the mixed waste to (l) acid wash, and (2) have the substitution for a non-radioactive cesium or cobalt change places. If, during the acid or water wash, the radioactive cesium falls off the oil (acidify to put into same oxidation state) , then non-radioactive cesium ion takes its place. All or some of these chemicals in the process can be used in the decontamination process.

The amounts of the chemicals used were less than one liter each, due to the fact that there were low levels of cesium, cobalt chloride or other carrier ion contamination. The hydrochloric acid added was approximately 250 milliliters per 800 gallons. The ferric chloride was approximately 500 milliliters. The cesium and cobalt chloride were approximately 125 milliliters or less per batch. These helped reduce the amount of radioactivity due to the ultimate switch at radioactive element bonding sites in the hazardous material.

The ferric chloride was used as a final flocculent/cleaner of the radioactive isotopes. • A 1 micron- or less finishing filter 23 was used to remove essentially all of the remaining activity and the flocculent from the hazardous material. The amounts of sodium EDTA and sodium hydroxide would vary depending on the amount of water which was found in the hazardous material being processed. Sodium EDTA and sodium hydroxide were also used. The amount of sodium EDTA was approximately 9 to 10 kilograms per 800 gallons and sodium hydroxide was roughly half of that for the optimum pH to be around 11. Sodium citrate was used in the charcoal filter 28 phase of the hazardous material for processing of water to eliminate organic products, if needed.

The main processing tank 11 was lined or surrounded with insulation to help with the prevention of heat loss.

Another step to the process was the addition of 10 to 20 gallons of water (the maximum should be 45 gallons) to the liquid hazardous material, namely, mixed waste, prior to or during the addition of the solid sodium EDTA and sodium hydroxide. Water added to a mixed waste without water enhances the process. This was an unusual step in the process since one would not normally add clean items to radioactive items, thus creating more radioactive, low level radioactive material, hazardous material or mixed waste.

The addition of the water could be to the main processing tank 11 at this stage or at the settling tank 31 phase earlier in the processing. This created a water washing instead of a normal acid washing due to the fact that acid is more difficult to dispose of in a radioactive mixed waste arena. The water allowed the radioactive isotopes to cling to that phase. It also allowed the entrained water to possibly cling to water molecules and thus eliminated entrained water. It was also used in the chemical phase in the main processing tank 11 to enhance the circulation of the chemicals, allowing the chemicals to travel more freely through the liquid hazardous material or mixed waste. This stage was primarily used in the hazardous material or mixed wastes that were water immiscible. When added to the main processing tank 11, water is added through the chemical add tank 19. When added to the settling tank 31, an additional supply is provided to the inlet line 36.

Once the chemicals have been added, the radioactivity tends to cling or jump into the water phase, or the water with the chemical phase, and can be removed via separation. At this point, once separated, the water phase was then neutralized with an acid and run through an evaporator or dehydrator 44 and sent out as a solid radioactive waste 45 as it contained no more hazardous waste properties and was a salt. Should this not be allowed, it could also be run through ion exchange and finer filtration to eliminate the salt prior to being run through the ion exchange.

The mixed waste which the chemicals have been recirculating through, chelating and rebonding the non- radioactive isotopes, was then run through the last stage or step of the process which is the finishing filters 23.

The finishing filters 23 can either be a water based or a non-water based filter. The filter 23, which is 1 micron absolute and submicronic, removed any additional water that was composed in the toxic mixed waste. At this point, the activity was also left inside the filter 23 as any of the finer particulate activity should have been removed via the separation and chemical addition.

Essentially, anything that remained was entrapped on the finishing or polishing filter 25. If the mixed waste was water based, the water based product could be run through a second chemical add tank 27 where sodium citrate would be added. Sodium citrate helps remove the radioactivity by enhancing the ability for the radioactivity in the water to adhere to a filtering media 28. Sodium citrate works well with charcoal and would thus be run through charcoal to remove any organic based contaminants in the water phase.

At this point, the activity was removed and the water based product was essentially just water. It was clean and could be run through any numerous amount of systems. It could run through ion exchange if there were any ionic elements that were still thought to be in it. If they were still radioactive, it could be run through radioactive/mixed wash processing systems.

An important independent phase for oil based liquid hazardous materials was heating to over 175° Fahrenheit. About 185° Fahrenheit to 190° Fahrenheit appeared to work the best. A recirculation and chemical addition phase of the processing was also independently important. This allowed the chemicals, including carrier chemicals and chelating agents, to be more active with the radioactive bonding sites.

Independently, the water addition was important. Water addition was included in the chemical phase. To the mixed waste which is water immiscible, the adding of the water enhanced the chemicals and chelating agents to bond more readily. It provided a good water washing. This allowed a lot of the activity to run through the water. This water was easily run through ion exchange (mixed beds) and the activity was then removed.

Also, independently, the adding of cobalt, cesium and ferric chloride or other carrier chemicals after water washing or slight acid washing often helped put a cesium, cobalt or iron element which is non- radioactive in the place of the radioactive element.

Final filtration or polishing filters-23 removed any of the last remaining particulate or colloidal phases of the radioactive isotopes within the mixed waste. This included the flocculents created by the chemical phase. The charcoal filter 28 and the mixed bed resin filters 35 and 18 which were used in separate stages or ases of this separation process can be interchangeable through a filter housing. Prior to running through the charcoal filter 28, the fluid is usually run through a submicron filter to eliminate any of the heavy particulates and allow for the liquid to be free of any contaminants which might affect the filter media, such as the charcoal or the resin.

The final process stage is the final sampling. The product is run through a gammaspectrophotometer at a thousand seconds. If activity was picked up, the decontamination process can be run again through the same steps as mentioned before. If activity was not detected, the product can either be resampled and checked again, or it can be classified as "clean" or free of radioactivity. End clean products, such as oil, can be reused or recycled for different purposes.

The above description is essentially related to oil-based liquid hazardous material. Not all the steps may be necessary for other liquid hazardous material which are not oil-based such as certain solvents or ethylene glycol. Thus, the filtration steps should be considered independently. Also, the water addition step should be considered independent. Likewise, the recirculation step is an independent step, as are the chelating step, the heating step, and the addition of chemicals independent steps. When these steps are considered selectively, together with different materials being treated, different degrees of effective treatment of the material is achieved. With oil-based material, the filtration, recirculating, heating, chelating and chemical addition steps were most effective.

Many other forms of the invention exist, each differing from the other in matters of detail only. For instance, although the invention is described with reference to batch processing between about 500 to 800 gallons of liquid hazardous material, the invention can operate with higher volumes of such material. As such, amounts between about 1,000 gallons and about 2,000 gallons can be handled by this procedure.

Continual heatering avoid heat loss and subsequent temperature drop. Continual heating causes the separation of the phases to be more effective. The ability of the chemicals to move freely through the mixed waste is also enhanced. By adding heating elements for substantially continual or regular heating within the main processing tank 11, the temperature would not decrease beyond a defined range, thus not effecting the processing, and the described benefits are achieved.

Radioactive air effluent is becoming a concern. The system with a scrubbing unit 101 allows the pressure of the entire system caused by the increase in temperature and the pump pressure to be bubbled through an acid bath 102 and then through a caustic bath 103 to neutralize the air effluent along line 104. The acid bath 102 permits the potential for water vapor (potentially comprised with Cesium) to be removed at the acid bath 102. The acid bath 102 and caustic bath 103 can also be used during the additions of the carrier chemicals and can be metered into the main processing tank 11 through line 105 and 106.

The scope of the present invention is to be determined solely by the appended claims.

Claims

CLAIMS :

1. A method of removing a radioactive contaminant from liquid hazardous material comprising: - directing liquid hazardous material into a processing tank, and circulating the liquid hazardous material between a filter medium and the processing tank thereby to remove radioactive particulates in the filter medium.

2. A method of removing radioactive contaminants from liquid hazardous material comprising: directing hazardous material into a processing tank, heating the liquid hazardous material, and circulating the heated liquid hazardous material between a filter medium and the processing tank thereby to remove radioactive particulates in the filter medium.

3. A method of removing radioactive contaminant from liquid hazardous material comprising: - directing the liquid hazardous material into a processing tank, heating the liquid hazardous material, circulating the heated liquid hazardous material between a filter medium and the processing tank thereby to remove in the filter medium radioactive particulates, and adding a chemical for enhancing the removal of radioactive particulates in the filter medium.

4. A method as claimed in claim 1 wherein, with about to 500 to about 800 gallons of liquid hazardous material, circulation is effected at a rate greater than about 50 gallons per minute.

5. A method as claimed in claim 4 wherein the circulation rate is greater than about 100 gallons per minut .

6. A method as claimed in claim 5 wherein the circulation rate is about 125 gallons per minute.

7. A method as claimed in claim 2 wherein heating is effected to a temperature of greater than about 50° Fahrenheit.

8. A method as claimed in claim 7 wherein the heating is effected to a temperature greater than about 100° Fahrenheit.

9. A method as claimed in claim 8 wherein the heating is effected to a temperature in a range between about 175° and 195° Fahrenheit.

10. A method as claimed in claim 2 wherein the liquid is an oil, including a proportion of water.

11. A method as claimed in claim 10 wherein the heating and circulation permits removal by filtration of water entrained in oil.

12. A method as claimed in claim 11 wherein filtration is effected in a range of about 50 microns and about 1 micron.

13. A method as claimed in claim 11 wherein filtration is effected by bag filters.

14. A method as claimed in claim 11 including adding a chemical for enhancing the removal of radioactive particulates.

15. A method as claimed in claim 3 wherein the chemical includes a chelating agent, the chelating agent being selectively EDTA and further being selectively a chelating agent in the sodium form.

16. A method as claimed in claim 15 including adding a pH adjusting chemical to obtain a pH range between about 9 and about 12 and selectively between about 10 and about 11.

17. A method as claimed in claim 15 including adding selectively a caustic neutralizing acid, being phosphoric or sulfuric acid, a chloride carrier chemical being selectively at least one of cesium chloride, cobalt chloride, or ferric chloride, and an acid wash chemical being selectively hydrochloric acid.

18. A method as claimed in claim 14 including selectively acid or water washing the liquid hazardous material thereby to effect transfer of a radioactive element from oil contained in the liquid hazardous material to a non-radioactive element, the transfer being of at least one of the elements of cesium, cobalt or iron.

19. A method as claimed in claim 14 including adding a flocculent chemical, such chemical being selectively ferric chloride for removing a radioactive element from the hazardous material.

20. A method as claimed in claim 19 including filtering the flocculent from the liquid hazardous material.

21. A method as claimed in claim 1 including adding a predetermined quantity of water to the liquid hazardous material.

22. A method as claimed in claim 2 including adding a predetermined quantity of water to the liquid hazardous material.

23. A method as claimed in claim 22 including adding a chemical for enhancing removal of radioactive particulates and wherein the water is added no later than the addition of the chemical.

24. A method as claimed in claim 23 wherein the water is added during the addition of the chemicals.

25. A method as claimed in claim 22 including adding a chemical for enhancing removal of radioactive particulates and wherein water is added prior to the addition of the chemical.

26. A method as claimed in claim 22 wherein, for processing about 500 to 800 gallons of liquid hazardous material, at least about 10 gallons of water is added.

27. A method as claimed in claim 26 wherein about 10 to 20 gallons of water is added.

28. A method as claimed in claim 26 wherein about 45 gallons of water is added.

29. A method as claimed in claim 22 including adding the water to the processing tank.

30. A method as claimed in claim 22 including adding the water to the liquid hazardous material before such material enters the processing tank.

31. A method as claimed in claim 22 wherein the addition of water effects a water wash of the liquid hazardous material whereby radioactive elements adhere to the added water.

32. A method as claimed in claim 31 wherein the liquid hazardous material includes oil with entrained water and wherein the added water permits water entrained in the oil to adhere to the added water.

33. A method as claimed in claim 31 wherein the water containing radioactive elements is separated from the liquid hazardous material.

34. A method as claimed in claim 33 including neutralizing water containing the radioactive elements and thereafter selectively subjecting the water to evaporation or dehydration thereby to obtain a solid radioactive waste.

35. A method as claimed in claim 21 including filtering the radioactive water in an ion exchange resin.

36. A method as claimed in claim 21 including directing liquid hazardous material from the processing tank to fine filtering for separating residual water and for entrapping radioactive elements in the fine filtering.

37. A method as claimed in claim 1 including directing the liquid hazardous material into a settling tank prior to directing the liquid hazardous material into the processing tank.

38. A method as claimed in claim 2 including directing the liquid hazardous material into a settling tank prior to directing the liquid hazardous material into the processing tank.

39. A method as claimed in claim 3 including directing the liquid hazardous material into a settling tank prior to directing the liquid hazardous material into the processing tank.

40. A method as claimed in claim 37 including filtering the liquid hazardous material prior to entry into the settling tank.

41. A method as claimed in claim 38 including filtering the liquid hazardous material prior to entry into the settling tank.

42. A method as claimed in claim 39 including filtering the liquid hazardous material prior to entry into the settling tank.

43. A method as claimed in claim 39 including directing water from the settling tank through an ion exchange resin mixed bed to remove radioactive elements in the ionic phase.

44. A method as claimed in claim 39 including directing water from the settling tank through an ion exchange resin mixed bed to remove radioactive elements in the ionic phase.

45. A method as claimed in claim 39 including directing water from the settling tank to an ion exchange resin mixed bed to remove radioactive elements in the ionic phase.

46. A method of removing radioactive contaminants from liquid hazardous material comprising directing liquid hazardous material into a settling tank, separating water from the liquid hazardous material in the settling tank, directing the remaining hazardous material to a processing tank, circulating the remaining liquid hazardous material through the processing tank, heating the remaining liquid hazardous material in the processing tank while such liquid hazardous material circulates through the tank, filtering the remaining liquid hazardous material during circulation through the tank, adding chemicals for enhancing the removal of radioactive particulates to the liquid circulating through the processing tank, filtering with finishing filters hazardous material as discharged from the processing tank thereby to remove particulate and colloidal radioactive elements from the discharged liquid hazardous material, and directing liquid substantially free of radioactive elements from the finishing filter for collection in a reservoir.

47. A method as claimed in claim 46 including adding water selectively to the liquid in the settling tank or the liquid in the processing tank.

48. A method as claimed in claim 46 wherein the chemicals include a chelating agent and a carrier to transfer the radioactive elements from the liquid hazardous material to the carrier while the carrier transfers non-radioactive elements to the liquid hazardous material.

49. A method as claimed in claim 47 including a carrier chemical wherein the liquid hazardous radioactive elements transfer from the liquid hazardous materials to the carrier chemicals and the carrier chemicals transfer non-radioactive elements to the liquid hazardous material.

50. A method of removing a radioactive contaminant from liquid hazardous material comprising directing the liquid hazardous material into a processing tank, circulating the liquid hazardous material between a filter medium and the processing tank thereby to remove radioactive particulates in the filter medium, pre- filtering the liquid hazardous material upstream of the processing tank with a filter coarser than the filter in the recirculating path thereby to remove radioactive contaminants from the liquid hazardous material and directing an outlet from the processing tank with the remaining liquid hazardous material after filtration in the recirculating filter to a finishing filter, and finish filtering the remaining hazardous material thereby to remove finer material containing radioactive elements.

51. A method as claimed in claim 50 wherein the pre-filter operates in the range of about 100 micron filtration, the recirculation filter operates in the range of between 5 micron and 1 micron filtration and the finishing filter operates in the range of about 1 micron filtration.

52. A method as claimed in claim 50 wherein the pre-filter is a bag filter, the recirculating filter is a bag filter, and the finishing filter is selectively a water absorption filter or an ion exchange resin.

53. A method as claimed in claim 50 including further filtering being effected after addition of a chemical additive to enhance filtration.

54. A method of removing radioactive contamination from liquid hazardous material comprising: directing the liquid hazardous material into a processing tank, circulating the liquid hazardous material between a filter medium and the processing tank thereby to remove in the ilter medium radioactive particulates, and adding a chemical for enhancing the removal of radioactive particulates in the filter medium.

55. A method as claimed in claim 54 including adding a predetermined amount of water to the liquid hazardous material.

56. Apparatus for removing radioactive contaminants from liquid hazardous material comprising a processing tank, means for directing liquid hazardous material into the processing tank, means for circulating liquid hazardous material through the processing tank, a filter medium in the circulation path for removing in this filter medium radioactive particulates.

57. Apparatus as claimed in claim 56 including heating means for heating the liquid hazardous material in the main processing tank.

58. Apparatus as claimed in claim 57 including a heater located in a liquid path recirculating liquid to the main processing tank.

59. Apparatus as claimed in claim 56 including a chemical addition tank for adding a chemical to the liquid recirculating in the main processing tank.

60. Apparatus as claimed in claim 56 including a pump for selectively recirculating liquid through the main processing tank, directing liquid through a heater to the main processing tank, and directing liquid through a chemical addition tank to the main processing tank.

61. Apparatus as claimed in claim 60 including a finishing filter downstream of the main processing tank and wherein the pump includes means for selectively directing liquid to the finishing filters.

62. Apparatus as claimed in claim 56 including selectively an evaporator or dehydrator located downstream the main processing tank, such evaporator or dehydrator acting to solidify liquid hazardous material directed from the main processing tank.

63. Apparatus as claimed in claim 60 including a further filter downstream the finishing filter, such further filter being a charcoal filter for removal of trace contaminants and including a second chemical addition tank between the finishing filter and the charcoal filter, such second chemical addition tank permitting the addition of a chemical for enhancement of the operation of the charcoal filter.

64. Apparatus as claimed claim 56 including a settling tank upstream of the processing tank.

65. Apparatus as claimed in claim 64 including the pre-filter located upstream of the settling tank, such pre-filter being for removal of coarser radioactive elements prior to introduction of the settling tank.

66. Apparatus as claimed in claim 65 including pump means for directing liquid from the settling tank to the main processing tank to an ion exchange mixed bed for removal of ionic phase radioactive elements.

67. Apparatus as claimed in claim 65 including an oily waste separator for removing oil from the settling tank and returning said oil to the settling tank.

68. Apparatus as claimed in claim 56 including means for adding water to the liquid hazardous material.

69. A method as claimed in claim 39 including directing water from the settling tank to an ion exchange resin mixed bed and then to a second chemical addition tank and to a charcoal filter for removing radioactive elements in the ionic phase and organics.

70. A method as claimed in claim 39 including directing water from the settling tank to a second chemical addition tank and then to a charcoal filter for removing organics and radioactive elements.

71. A method as claimed in claim 39 including selectively bypassing the settling tank and directing liquid to the processing tank.

72. A method as claimed in claim 50 including directing liquid through finishing filters and bypassing a second chemical tank and charcoal filter and being selectively directed to a reservoir for clean liquid.

73. A method as claimed in claim 1 including processing liquid in a batch amount of between 500 gallons and 2,000 gallons.

74. A product treated by the method of claim 1.

75. A product treated by the method of claim 2.

76. A product treated by the method of claim 3.

77. A product treated by the method of claim 46.

78. A product treated by the method of claim 50.

79. A product treated by the method of claim 54.

80. A method as claimed in claim 2 wherein the radioactive particulates removed include at least cobalt, and selectively cobalt 60.

81. Apparatus as claimed in claim 56 includes means for removing at least cobalt, and selectively cobalt 60.

82. A product treated by the method of claim 80,

83. A method as claimed in claim 2 including substantially continually heating the liquid hazardous material to maintain a defined temperature.

84. A method as claimed in claim 2 including treating the material in an acid and a caustic scrubber thereby to remove radioactive material from air effluent.

85. Apparatus as claimed in claim 50 including heating means in the processing tank, the heating elements being for maintaining the temperature in a defined range.

86. Apparatus as claimed in claim 56 including scrubbing means for removing radioactive material from air effluent.