USH970H - Integrated decontamination process for metals - Google Patents
Integrated decontamination process for metals Download PDFInfo
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- USH970H USH970H US07/363,019 US36301989A USH970H US H970 H USH970 H US H970H US 36301989 A US36301989 A US 36301989A US H970 H USH970 H US H970H
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B9/00—General processes of refining or remelting of metals; Apparatus for electroslag or arc remelting of metals
- C22B9/10—General processes of refining or remelting of metals; Apparatus for electroslag or arc remelting of metals with refining or fluxing agents; Use of materials therefor, e.g. slagging or scorifying agents
- C22B9/106—General processes of refining or remelting of metals; Apparatus for electroslag or arc remelting of metals with refining or fluxing agents; Use of materials therefor, e.g. slagging or scorifying agents the refining being obtained by intimately mixing the molten metal with a molten salt or slag
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B9/00—General processes of refining or remelting of metals; Apparatus for electroslag or arc remelting of metals
- C22B9/10—General processes of refining or remelting of metals; Apparatus for electroslag or arc remelting of metals with refining or fluxing agents; Use of materials therefor, e.g. slagging or scorifying agents
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25C—PROCESSES FOR THE ELECTROLYTIC PRODUCTION, RECOVERY OR REFINING OF METALS; APPARATUS THEREFOR
- C25C1/00—Electrolytic production, recovery or refining of metals by electrolysis of solutions
Definitions
- This invention relates to decontamination of metals, particularly metals that are used in the nuclear energy industry contaminated with radioactive material.
- Postutilization storage costs would also be less since material that would ordinarily be placed in a containment repository could be reused. This avoids the need for both preliminary containment processing as well as continued inventory and control of the waste. Circumventing waste containment also has an environmental payoff since storage of contaminated materials risks the danger of their spread by water runoff, wind or natural catastrophe.
- An additional object of this invention is to provide a process for minimizing the bulk waste that must be contained as a result of radioactive contamination of reactor material.
- a further object of this invention is to provide a process that allows the reprocessing of contaminated materials in a economical manner so that recycling will be cost effective. Additional objects, advantages and novel features of the invention will be set forth in part in the description which follows, and in part will become apparent to those skilled in the art upon examination of the following or may be learned by practice of the invention. The objects and advantages of the invention may be realized and attained by means of the instrumentalities and combinations particularly pointed out in the appended claims.
- the process of this invention may comprise, first, separating the contaminated material into a first batch that contains metals that can be electrowon from aqueous electrolyte and a second batch that contains metals that cannot be electrowon from aqueous electrolyte, second, melt refining the material thus acquiring preliminary material that is partially decontaminated, third, electrorefining said first batch and melt refining said second batch.
- This integrated process using a combination of melt refining and electrorefining, is less expensive and produces a higher quality product than melt refining alone.
- FIG. 1 is a schematic that represents the process steps of the integrated decontamination process for metals.
- FIG. 2 is a schematic that represents the process steps of Melt Refining Stage One.
- FIG. 3 is a schematic that represents the specific electrorefining process in the semicontinuous operating mode.
- FIG. 4 is a eutectic diagram of the iron-uranium system.
- FIG. 5 is a schematic that represents a detailed description of the Stage Two Melt Refining Process.
- FIG. 1 outlines the process that comprises basically three procedures: Melt Refining Stage One, an inorganic solvent extraction; Melt Refining Stage Two, a facilitated extraction; and Electrorefining. Before determining which processes are to be used it is necessary to classify the contaminated feedstocks as shown in Table 1.
- the strategy for decontamination entails reducing high levels of contamination in the raw feed, in both quantity and activity, by inorganic solvent extraction in Melt Refining Stage One. Although this extraction is not quantitative, it will reduce reagent consumption, energy costs and radioactivity levels for the more intensive polishing stages.
- the next step is to eliminate the contamination quantitatively in the polishing steps of Melt Refining Stage Two and Electrorefining.
- Electrorefining is the preferred process polishing operation where applicable for several reasons. It is less expensive than melt refining since it operates at a lower temperature, it requires less capital expenditure for equipment and it produces smaller quantities of radionuclide waste which requires disposal. Furthermore, it is quantitative as a function of reduction potential in the electromotive series unlike other processes that leave measurable levels of contaminants behind. Additionally, it provides a more valuable product since it not only decontaminates but also results in a higher purity metal than can be achieved by melt refining.
- decontamination is effective based on their reduction potentials relative to the radionuclides as the series in Table 2 shows.
- Melt Refining Stage One is essentially an inorganic solvent extraction for the primary cut. The extraction occurs between two phases, the raffinate or metal phase and the extract or flux phase. In the absence of an external driving force, such as facilitated transport, an equilibrium distribution is the best that can be expected. Efficiency is determined by that distribution. Since the process does not result in quantitative decontamination, polishing processes, such as Melt Refining Stage Two and Electrorefining, will be required to treat Stage One product to generate decontaminated material that is acceptable for recycle.
- FIG. 2 is a schematic that describes the process of Melt Refining Stage One.
- the feedstock is masticated or comminuted to insure intimate mixing and contact with the flux.
- Melt Refining Stage One must address a wide range of metals as an initial decontamination stage. Therefore, it must also address a range of operating temperatures and extraction flux compositions. Both are selected as a function of the specific metal to be decontaminated following the guidelines of Table 3.
- Flux components from Table 3 are blended separately to appropriate composition. Flux and metal may be mixed in the solid phase and heated to temperature in the furnace. Alternatively, they may be heated to temperature and mixed in the molten state. Agitation and a nonoxidizing atmosphere are required in the melting furnace design for effective phase contact. The slag and melt phases are separated and the melt is cast into ingots for cooling. This stage of extraction can be repeated as required for second or third stages of extraction to reduce the contamination levels further prior to the polishing stages. The extract phase or product flux is likely to be highly contaminated and will require encapsulation on glass or cement for disposal as TRU (transuranic) waste. Table 4 shows typical single stage decontamination results. Stage One Melt Refining will generate Class 2 or Class 4 material.
- Electrorefining addresses Class 2 materials with Class 3 materials added.
- Melt Refining Stage Two addresses Class 4 materials.
- the major feedstocks are Class 2 metals resulting from Melt Refining Stage One.
- Class 3 materials contaminated metal compounds whose metals can by won from aqueous electrolytes, are not only decontaminated by the electrorefining process, but are reduced to the base metal increasing product value.
- Typical feedstock contamination levels are shown in Table 4.
- the aqueous electromotive series in Table 2 is the basis for such separations.
- Electrorefining has two modes of operation. First is the batch mode where contaminated metal dissolves in the electrolyte which serves as both transport medium and metal source. A blank anode distributes the current and the cathodic product is removed. This is the required operating mode to decontaminate metal compounds. The other is the semicontinuous mode where contaminated metal is cast into anodes. The metal is dissolved anodically during the cell operation and plated out at the cathode. In this mode the electrolyte is strictly a transport medium.
- FIG. 3 assuming the semicontinuous operating mode. Contaminated feedstocks are cast into anodes, both for cell operation and for precharging the electrolyte to the ranges shown in Table 5.
- metal product may be recycled for other uses or subjected to an additional purification process such as zone melting to improve its chemical purity.
- Metal tails from this zone refining process which have already been decontaminated can be sold as a lower purity grade or recycled to the anode casting process.
- the spent electrolyte is partially neutralized to precipitate the metal contaminants as a sludge.
- the sludge is filtered, dewatered, and encapsulated for disposal in either cement or glass.
- the filtrate is passed through a demineralizer and recycled to the process.
- Stage Two Melt Refining will address Class 4 metals such as zirconium, aluminum, titanium, hafnium and others which cannot be won from aqueous electrolytes, achieving the quantitative removal of contaminants by facilitated transport extraction.
- alloying elements are intentionally added to the melt. Their objective is to complex the radionuclides present in the melt, converting them to species more readily extracted by the flux. This process both shifts equilibrium and improves transport kinetics.
- a primary alloying agent is iron, the behavior of which is depicted in FIG. 4.
- Other elements such as zirconium, titanium, niobium or others can be added to improve system performance and product purity.
- the metal can be added to the melt in pure form or its oxide may be reduced in the furnace carbothermically by reaction with carbon at furnace temperature.
- the scrubbing flux may be selected from the list of candidates in Table 4, or others may be used.
- borosilicate glass is an effective flux for nickel decontamination in Stage One Melt Refining. CaO/Fe 2 O 3 /SiO 2 is preferred for Stage Two decontamination.
- FIG. 5 is a detailed description of the Stage Two Melt Refining Process.
- Table 7 demonstrates its efficiency for the specific case of nickel decontamination relative to the Stage One Melt Refining.
- contaminated metal is comminuted in a mastication process and blended with flux and alloying agent.
- flux and alloy agent could be melted individually, brought to the same temperature and blended in the furnace.
- the flux mass ranges from 10% to 200% of the metal mass.
- the high flux level favors more effective decontamination by diluting the extract phase.
- the lower level reduces the amount of waste slag which must be treated in waste management.
- the alloy reagent should be present as 110% or more of the theoretical requirement, based on the stoichiometry of the existing contaminants.
- the materials are fired in an induction furnace for 10-60 minutes. Agitation is recommended; an inert or reducing atmosphere is required.
- the furnace temperature is a direct function of the melting points of the metal, flux, and alloy reagent. In the case of the system Ni, Fe 2 O 3 -CaO-SiO 2 and iron metal, the recommended temperature is in excess of 1550° to 1600° C.
- wastes from this process have concentrated radionuclides as a result of the decontamination process. These wastes consist of Stage One Melt Refining borosilicate flux, Stage Two Melt Refining Fe 2 O 3 -SiO 2 -CaO flux, and electrorefining spent electrolyte sludge. These wastes are encapsulated in glass or cement as required by their level of residual contamination.
Abstract
An integrated process for decontamination of metals, particularly metals that are used in the nuclear energy industry contaminated with radioactive material. The process combines the processes of electrorefining and melt refining to purify metals that can be decontaminated using either electrorefining or melt refining processes.
Description
This invention was developed under a contract with the U.S. Department of Energy, Contract No. DE-AC05-86-OR-21670.
This invention relates to decontamination of metals, particularly metals that are used in the nuclear energy industry contaminated with radioactive material.
The nuclear community, both commercial and governmental, contaminates a large quantity of metals and alloys annually. Some of the contamination is only surface while other is blended homogeneously through the metal. Rather than discard the contaminated materials, there are several incentives to decontaminate them for recycle.
There are economic motivations that make recycling attractive. If an inexpensive method for decontamination could be found, high quality material could be made at a fraction of the cost that conversion from ore would require. Strategic resources such as cobalt, chromium, nickel, aluminum, zirconium and titanium could be recovered.
Postutilization storage costs would also be less since material that would ordinarily be placed in a containment repository could be reused. This avoids the need for both preliminary containment processing as well as continued inventory and control of the waste. Circumventing waste containment also has an environmental payoff since storage of contaminated materials risks the danger of their spread by water runoff, wind or natural catastrophe.
It is important that any process developed must be able to remove contaminated materials not only from the surface of metals but also from within those metals which experience homogeneous contamination.
In view of the above needs, it is an object of this invention to provide a process that decontaminates metals that are homogeneously contaminated with radioactive material.
It is another object of this invention to provide a process for recycling valuable and strategic materials that are contaminated due to exposure to nuclear reactor environments.
An additional object of this invention is to provide a process for minimizing the bulk waste that must be contained as a result of radioactive contamination of reactor material.
A further object of this invention is to provide a process that allows the reprocessing of contaminated materials in a economical manner so that recycling will be cost effective. Additional objects, advantages and novel features of the invention will be set forth in part in the description which follows, and in part will become apparent to those skilled in the art upon examination of the following or may be learned by practice of the invention. The objects and advantages of the invention may be realized and attained by means of the instrumentalities and combinations particularly pointed out in the appended claims.
To achieve the foregoing and other objects and in accordance with the purpose of the present invention, as embodied and broadly described herein, the process of this invention may comprise, first, separating the contaminated material into a first batch that contains metals that can be electrowon from aqueous electrolyte and a second batch that contains metals that cannot be electrowon from aqueous electrolyte, second, melt refining the material thus acquiring preliminary material that is partially decontaminated, third, electrorefining said first batch and melt refining said second batch. This integrated process, using a combination of melt refining and electrorefining, is less expensive and produces a higher quality product than melt refining alone.
FIG. 1 is a schematic that represents the process steps of the integrated decontamination process for metals.
FIG. 2 is a schematic that represents the process steps of Melt Refining Stage One.
FIG. 3 is a schematic that represents the specific electrorefining process in the semicontinuous operating mode.
FIG. 4 is a eutectic diagram of the iron-uranium system.
FIG. 5 is a schematic that represents a detailed description of the Stage Two Melt Refining Process.
FIG. 1 outlines the process that comprises basically three procedures: Melt Refining Stage One, an inorganic solvent extraction; Melt Refining Stage Two, a facilitated extraction; and Electrorefining. Before determining which processes are to be used it is necessary to classify the contaminated feedstocks as shown in Table 1.
TABLE 1
______________________________________
MATERIAL CLASSIFICATION FOR
DECONTAMINATION PROCESSING
MATERIAL PROCESS MATERIAL
CLASS DESCRIPTION OPTION ORIGIN
______________________________________
1 Highly Melt Refining Outside*
contaminated Stage One, as a
gross reduction
in the contamin-
ation level.
2 Low contamina-
Electrorefining
Melt Refining
tion metal which Stage One, or
can be electrowon outside
from aqueous process**
electrolytes
3 Low contamina-
Electrorefining
Outside
tion metal com- process**
pounds which can
be electrowon
from aqueous
electrolytes
4 Low contamina-
Metal Refining
Melt Refining
tion metal which
Stage Two with
Stage One, or
cannot be electro-
facilitated trans-
outside
won from aqueous
port process**
electrolytes
______________________________________
*Highly contaminated feedstock from outside sources such as military or
commercial waste.
**Lowly or moderately contaminated feedstock from outside sources.
The strategy for decontamination entails reducing high levels of contamination in the raw feed, in both quantity and activity, by inorganic solvent extraction in Melt Refining Stage One. Although this extraction is not quantitative, it will reduce reagent consumption, energy costs and radioactivity levels for the more intensive polishing stages. The next step is to eliminate the contamination quantitatively in the polishing steps of Melt Refining Stage Two and Electrorefining.
Selecting the proper polishing step depends on whether the metal can be electrowon from aqueous solution. Electrorefining is the preferred process polishing operation where applicable for several reasons. It is less expensive than melt refining since it operates at a lower temperature, it requires less capital expenditure for equipment and it produces smaller quantities of radionuclide waste which requires disposal. Furthermore, it is quantitative as a function of reduction potential in the electromotive series unlike other processes that leave measurable levels of contaminants behind. Additionally, it provides a more valuable product since it not only decontaminates but also results in a higher purity metal than can be achieved by melt refining.
For metal such as nickel, copper, cobalt and iron which can be electrowon from aqueous solution, decontamination is effective based on their reduction potentials relative to the radionuclides as the series in Table 2 shows.
TABLE 2
______________________________________
REDOX POTENTIAL SERIES FOR AQUEOUS
ELECTROREFINING
Oxidation-Reduction Couples in Acid Solutions
______________________________________
Table Reference Voltage:
H.sub.2 ⃡ 2H.sup.+ + 2e.sup.- at 0
______________________________________
volts
Li = Li(I) + e.sup.-
3.045 = E
Ra = Ra(II) + 2e.sup.-
2.92
Ba = Ba(II) + 2e.sup.-
2.90
Sr = Sr(II) + 2e.sup.-
2.89
Am = Am(III) + 3e.sup.-
2.32
Pu = Pu(III) + 3e.sup.-
2.07
Th = Th(IV) + 4e .sup.-
1.90
Np = Np(III) + 3e.sup.-
1.86
U = U(III) + 3 e.sup.-
1.80
Hf = Hf(IV) + 4e.sup.-
1.70
Ti = Ti(II) + 2e.sup.-
1.63
Zr = Zr(IV) + 4e .sup.-
1.53
Cr = Cr(III) + 3e.sup.-
0.75
Voltage of 1 volt
Fe = Fe(II) + 2e.sup.-
0.44
Co = Co(II) + 2e.sup.-
0.277
Ni = Ni(II) + 2e.sup.-
0.25 v
Cu = Cu(II) + 2e.sup.-
-0.337 v
______________________________________
At pH 2.36, -0.8 volts versus the standard calomel electrode, and dilute
sulfuric acid, a 95% yield was reported with a 65 minute deposition time
for technetium. The same system wins plutonium at a voltage of +.56 volts
versus the standard calomel electrode. Therefore, technetium would be won
from sulfuric acid solution at 0.71 volts against the hydrogen reference
above.
However, many metal such as zirconium, hafnium and titanium, require molten salt electrolysis at 150°-1000° C. Furthermore, insufficient difference in reduction potentials between the titanium group and actinides exists to effect decontamination. Thus, an alternative approach, such as Melt Refining Stage Two with facilitated transport, is required to address these materials. The combination of Electrorefining and Melt Refining Stage Two allows adequate process flexibility to address most metals.
Melt Refining Stage One is essentially an inorganic solvent extraction for the primary cut. The extraction occurs between two phases, the raffinate or metal phase and the extract or flux phase. In the absence of an external driving force, such as facilitated transport, an equilibrium distribution is the best that can be expected. Efficiency is determined by that distribution. Since the process does not result in quantitative decontamination, polishing processes, such as Melt Refining Stage Two and Electrorefining, will be required to treat Stage One product to generate decontaminated material that is acceptable for recycle. FIG. 2 is a schematic that describes the process of Melt Refining Stage One.
The feedstock is masticated or comminuted to insure intimate mixing and contact with the flux. Melt Refining Stage One must address a wide range of metals as an initial decontamination stage. Therefore, it must also address a range of operating temperatures and extraction flux compositions. Both are selected as a function of the specific metal to be decontaminated following the guidelines of Table 3.
TABLE 3
__________________________________________________________________________
TYPICAL STAGE ONE MELT REFINING CONDITIONS
Typical
Temp- Equilibrium
erature Coefficient
Metal C. Flux Composition λ = [U]slag/[U]melt
__________________________________________________________________________
Stainless
1600 25% CaO, 75% SiO.sub.2
226
steel
Nickel
1550 Borosilicate Glass 77
Mild steel
mp +100
60% CaO, 10% SiO.sub.2, 30% Fe.sub.2 O.sub.3
583
Copper
1250 50% SiO.sub.2, 25% CaO, 25% A1.sub.2 O.sub.3
718
Aluminum
1300 CaF.sub.2 810
Lead 1200 80% Na.sub.2 CO.sub.3, 10% NaNO.sub.3, 10% PbO
433
Tin 1200 45% SiO.sub.2, 30% CaO, 20% Al.sub.2 O.sub.3, 5% Fe.sub.2
O.sub.3 392
Zinc 800 50% NaNO.sub.3, 45% NaCl, 5% Fe.sub.2 O.sub.3
˜8
Lead Tin
80-20 45% SiO.sub.2, 30% CaO, 20% Al.sub.2 O.sub.3, 5% Fe.sub.2
O.sub.3 >1500
50-50 -- <˜1
__________________________________________________________________________
Flux components from Table 3 are blended separately to appropriate composition. Flux and metal may be mixed in the solid phase and heated to temperature in the furnace. Alternatively, they may be heated to temperature and mixed in the molten state. Agitation and a nonoxidizing atmosphere are required in the melting furnace design for effective phase contact. The slag and melt phases are separated and the melt is cast into ingots for cooling. This stage of extraction can be repeated as required for second or third stages of extraction to reduce the contamination levels further prior to the polishing stages. The extract phase or product flux is likely to be highly contaminated and will require encapsulation on glass or cement for disposal as TRU (transuranic) waste. Table 4 shows typical single stage decontamination results. Stage One Melt Refining will generate Class 2 or Class 4 material.
TABLE 4
______________________________________
TYPICAL MELT REFINING DECONTAMINATION
RESULTS
Product Ingot
Direct Radiation
U Content, ppm*
Alpha d/m/200 cm.sup.2 **
Material Avg. Low High Avg. Low High
______________________________________
Common Steel
0.4 0.00 3.50 0 -- --
Stainless Steel
0.6 0.01 3.20 100 75 120
Ni-bearing
0.5 0.02 2.38 100 100 100
Steel
Nickel 1.25 0.9 1.6 120 100 200
Monel (Ni 0.5 0.01 4.00 -- -- --
Alloy)
Copper 0.4 0.01 2.50 100 100 100
Brass 0.4 0.01 2.50 -- -- --
Yellow Brass
2.1 0.30 3.20 -- -- --
Bronze 0.3 0.04 1.20 -- -- --
Aluminum 200 3 1400 3870 2000 6800
______________________________________
*Data primarily from Oak Ridge Y12 plant except for aluminum data which i
from Goodyear Atomic Corporation; ppm = parts per million by weight =
micrograms per gram.
**Data is primarily from Klevin Harris, Nucleonics 14, No. 4, pp. 936
(April 1956). Caution: values may not relate directly with ppm column
data; values in disintegrations per minute per 100 square centimeters.
Electrorefining addresses Class 2 materials with Class 3 materials added. Melt Refining Stage Two addresses Class 4 materials.
The major feedstocks are Class 2 metals resulting from Melt Refining Stage One. Class 3 materials, contaminated metal compounds whose metals can by won from aqueous electrolytes, are not only decontaminated by the electrorefining process, but are reduced to the base metal increasing product value. Typical feedstock contamination levels are shown in Table 4. The aqueous electromotive series in Table 2 is the basis for such separations.
Electrorefining has two modes of operation. First is the batch mode where contaminated metal dissolves in the electrolyte which serves as both transport medium and metal source. A blank anode distributes the current and the cathodic product is removed. This is the required operating mode to decontaminate metal compounds. The other is the semicontinuous mode where contaminated metal is cast into anodes. The metal is dissolved anodically during the cell operation and plated out at the cathode. In this mode the electrolyte is strictly a transport medium.
The specific process description follows FIG. 3 assuming the semicontinuous operating mode. Contaminated feedstocks are cast into anodes, both for cell operation and for precharging the electrolyte to the ranges shown in Table 5.
TABLE 5
______________________________________
TYPICAL ELECTROREFINING CONDITIONS
General Conditions for Iron, Copper, Cobalt and Nickel
______________________________________
pH 2 to 5.2
Temperature 25 to 65° C.
Voltage less than .5 to
.6 volts relative to H.sub.2
reduction potential
Specific Conditions
Current Density: 5-500 amp/dm.sup.2
Iron: .44v Ni: .25v Co: .28v Cu: .34 v
Metal Sulfate: 5-60 gm/L as metal
Metal Chloride: 0-40 gm/L
Boric Acid: 20-50 gm/L
Sodium Sulfate:
0 to 60 gm/L
______________________________________
If the metal compounds are to be decontaminated and won by the system, these are dissolved directly to form the electrolyte feedstock. Anodes, seed cathode, and feedstock electrolyte are changed to the electrorefining cell for operation at conditions at set forth in Table 5. On recovery, the cathode product is washed with a mild acid to remove residual electrolyte adhering to its surface. Results of this process are set forth in Table 6.
TABLE 6
______________________________________
NICKEL PURIFICATION RESULTS BY
ELECTROREFINING
______________________________________
Conditions
Temperature: 25° C.
Voltage: 1 v
Current Density: .04 amps/cm.sup.2
Residence Time: 6 hours
______________________________________
Chemical Analysis
Target Product Feed
Metals (wt %) (wt %) (wt %)
______________________________________
Ni 99.9 99.97** 99.90
Al NA 0.01 0.01
Co NA 0.0001 0.0001
Cr NA 0.01 0.01
Cu .005 0.0067 0.0059
Fe .002 0.55* 0.045
Mn NA 0.0007* 0.0001
Ti -- 0.019 0.044
______________________________________
Experimental Conditions
Example 1: 25° C.
1 volt 6 hours residence time
.026 amps/cm.sup.2
Example 2: 25° C.
1 volt 6 hours residence time
.040 amps/cm.sup.2
______________________________________
Feedstock Analysis
Westinghouse Product Results
AESD Oak Ridge Example 1
Example 2
Component
(PPM) (PPM) (PPM) (PPM)
______________________________________
Np.sup.237
BDL BDL BDL BDL
Pu.sup.239
BDL BDL BDL BDL
Tc.sup.99
.31 ± .01
.19 .65 ± .01
.42 ± .01
U.sup.235
BDL 1.04% U BDL BDL
U.sub.total
1.2 ± .3
13 *** BDL
______________________________________
*Presumed to be due to the partial dissolution of stainless electrode
leads resulting from electrolyte splashing and washing across the
electrodes.
**Eliminates the iron and manganese impurities resulting from splash.
***Not available due to insufficient sample
NA Not Analyzed
BDL Below Detectable Limit
At this stage the metal product may be recycled for other uses or subjected to an additional purification process such as zone melting to improve its chemical purity. Metal tails from this zone refining process which have already been decontaminated can be sold as a lower purity grade or recycled to the anode casting process.
The spent electrolyte is partially neutralized to precipitate the metal contaminants as a sludge. The sludge is filtered, dewatered, and encapsulated for disposal in either cement or glass. The filtrate is passed through a demineralizer and recycled to the process.
Stage Two Melt Refining will address Class 4 metals such as zirconium, aluminum, titanium, hafnium and others which cannot be won from aqueous electrolytes, achieving the quantitative removal of contaminants by facilitated transport extraction. Here alloying elements are intentionally added to the melt. Their objective is to complex the radionuclides present in the melt, converting them to species more readily extracted by the flux. This process both shifts equilibrium and improves transport kinetics.
A primary alloying agent is iron, the behavior of which is depicted in FIG. 4. Other elements such as zirconium, titanium, niobium or others can be added to improve system performance and product purity. The metal can be added to the melt in pure form or its oxide may be reduced in the furnace carbothermically by reaction with carbon at furnace temperature. The scrubbing flux may be selected from the list of candidates in Table 4, or others may be used. For example, borosilicate glass is an effective flux for nickel decontamination in Stage One Melt Refining. CaO/Fe2 O3 /SiO2 is preferred for Stage Two decontamination.
FIG. 5 is a detailed description of the Stage Two Melt Refining Process. Table 7 demonstrates its efficiency for the specific case of nickel decontamination relative to the Stage One Melt Refining.
TABLE 7
______________________________________
DECONTAMINATION PERFORMANCE IN MELT
REFINING FOR NICKEL
Experimental Results
Feedstock
Temperature ≧1550° C.
Analysis Westinghouse
DOE Stage One Stage Two
Component (ppm) (ppm) (ppm)
______________________________________
Np.sup.237
BDL BDL BDL
Pu.sup.239
BDL BDL BDL
Tc.sup.99 .19 .25 .35
U.sup.235 BDL BDL BDL
U.sub.total
1.3 1.1 ± .5
BDL
Nl balance balance balance
Al <0.01 <0.01 <0.01
Co <0.0001 <0.0001 <0.0001
Cr <0.01 <0.01 <0.01
Cu <0.0059 0.0057 0.0058
Fe 0.045 0.048 0.93
Mn <0.0001 0.0003 0.0002
Ti 0.044 0.024 0.013
Flux Borosilicate
CaO/Fe.sub.2 O.sub.3 /SiO.sub.2
λw** ˜2.5 3.4/BDL
Flux Negligible Significant
Interaction Producing
with Crucible Metallic Iron
______________________________________
BDL = Below Detectable Limits 0
λw = Conc. Slag/Conc. Melt
In the process contaminated metal is comminuted in a mastication process and blended with flux and alloying agent. Alternatively metal, flux and alloy agent could be melted individually, brought to the same temperature and blended in the furnace. The flux mass ranges from 10% to 200% of the metal mass. The high flux level favors more effective decontamination by diluting the extract phase. The lower level reduces the amount of waste slag which must be treated in waste management. The alloy reagent should be present as 110% or more of the theoretical requirement, based on the stoichiometry of the existing contaminants.
The materials are fired in an induction furnace for 10-60 minutes. Agitation is recommended; an inert or reducing atmosphere is required. The furnace temperature is a direct function of the melting points of the metal, flux, and alloy reagent. In the case of the system Ni, Fe2 O3 -CaO-SiO2 and iron metal, the recommended temperature is in excess of 1550° to 1600° C.
On cooling the furnace charge is tapped and separated. The slag proceeds to a glass or cement encapsulation process for waste management. The metal melt is poured into molds to form ingot. Finally an additional stage of zone refining can be applied to this stage as well for the specific purpose of improving chemical purity of the product.
All wastes from this process have concentrated radionuclides as a result of the decontamination process. These wastes consist of Stage One Melt Refining borosilicate flux, Stage Two Melt Refining Fe2 O3 -SiO2 -CaO flux, and electrorefining spent electrolyte sludge. These wastes are encapsulated in glass or cement as required by their level of residual contamination.
Claims (1)
1. A process for removing radioactive contamination from metals comprising:
a first step comprising melt refining contaminated material resulting in a metal phase and a flux phase;
separating said metal phase into a first batch and a second batch, said first batch being targeted for removal of specific metals that can be electrowon from aqueous electrolyte and said second batch being targeted for removal of specific metals that cannot be electrowon from aqueous electrolyte;
a second step comprising electrorefining said first batch; and a third step comprising melt refining said second batch.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US07/363,019 USH970H (en) | 1989-06-08 | 1989-06-08 | Integrated decontamination process for metals |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US07/363,019 USH970H (en) | 1989-06-08 | 1989-06-08 | Integrated decontamination process for metals |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| USH970H true USH970H (en) | 1991-10-01 |
Family
ID=23428443
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| US07/363,019 Abandoned USH970H (en) | 1989-06-08 | 1989-06-08 | Integrated decontamination process for metals |
Country Status (1)
| Country | Link |
|---|---|
| US (1) | USH970H (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5348567A (en) * | 1992-11-17 | 1994-09-20 | Clyde Shaw Limited | Decontamination method |
| US5724669A (en) * | 1996-10-15 | 1998-03-03 | Snyder; Thomas S. | Metal decontamination process and systems for accomplishing same |
| US20130216016A1 (en) * | 2010-08-25 | 2013-08-22 | Commissariat A L'energie Atomique Et Aux Energies Alternatives | Device for Mitigating Serious Accidents for a Nuclear Fuel Assembly, With Improved Effectiveness |
| US20150083599A1 (en) * | 2013-09-23 | 2015-03-26 | Sms Meer Gmbh | Method and system for the production of semi-finished copper products as well as method and apparatus for application of a wash |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2111575A (en) | 1936-07-18 | 1938-03-22 | Nassau Smelting & Refining Com | Refining of nonferrous metals |
| US2393582A (en) | 1942-08-08 | 1946-01-29 | Nat Lead Co | Method for utilizing iron chloride liquors |
| US4351705A (en) | 1981-06-30 | 1982-09-28 | Amax Inc. | Refining copper-bearing material contaminated with nickel, antimony and/or tin |
| US4395367A (en) | 1981-11-17 | 1983-07-26 | Rohrmann Charles A | Process for treating fission waste |
-
1989
- 1989-06-08 US US07/363,019 patent/USH970H/en not_active Abandoned
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2111575A (en) | 1936-07-18 | 1938-03-22 | Nassau Smelting & Refining Com | Refining of nonferrous metals |
| US2393582A (en) | 1942-08-08 | 1946-01-29 | Nat Lead Co | Method for utilizing iron chloride liquors |
| US4351705A (en) | 1981-06-30 | 1982-09-28 | Amax Inc. | Refining copper-bearing material contaminated with nickel, antimony and/or tin |
| US4395367A (en) | 1981-11-17 | 1983-07-26 | Rohrmann Charles A | Process for treating fission waste |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5348567A (en) * | 1992-11-17 | 1994-09-20 | Clyde Shaw Limited | Decontamination method |
| US5724669A (en) * | 1996-10-15 | 1998-03-03 | Snyder; Thomas S. | Metal decontamination process and systems for accomplishing same |
| US20130216016A1 (en) * | 2010-08-25 | 2013-08-22 | Commissariat A L'energie Atomique Et Aux Energies Alternatives | Device for Mitigating Serious Accidents for a Nuclear Fuel Assembly, With Improved Effectiveness |
| US20150083599A1 (en) * | 2013-09-23 | 2015-03-26 | Sms Meer Gmbh | Method and system for the production of semi-finished copper products as well as method and apparatus for application of a wash |
| US9994965B2 (en) * | 2013-09-23 | 2018-06-12 | Sms Group Gmbh | Method and system for the production of semi-finished copper products as well as method and apparatus for application of a wash |
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