CN117778766A - Method for extracting and separating minor actinides by using strontium americium recovery process - Google Patents
Method for extracting and separating minor actinides by using strontium americium recovery process Download PDFInfo
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- 229910052768 actinide Inorganic materials 0.000 title claims abstract description 71
- 150000001255 actinides Chemical class 0.000 title claims abstract description 63
- 238000000034 method Methods 0.000 title claims abstract description 55
- -1 strontium americium Chemical compound 0.000 title claims abstract description 39
- 238000011084 recovery Methods 0.000 title claims abstract description 19
- 239000012074 organic phase Substances 0.000 claims abstract description 123
- 229910052695 Americium Inorganic materials 0.000 claims abstract description 90
- LXQXZNRPTYVCNG-UHFFFAOYSA-N americium atom Chemical compound [Am] LXQXZNRPTYVCNG-UHFFFAOYSA-N 0.000 claims abstract description 83
- 239000008346 aqueous phase Substances 0.000 claims abstract description 72
- 239000007788 liquid Substances 0.000 claims abstract description 60
- 239000012071 phase Substances 0.000 claims abstract description 51
- 238000000605 extraction Methods 0.000 claims abstract description 46
- 238000005406 washing Methods 0.000 claims abstract description 44
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 40
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 37
- 229910052746 lanthanum Inorganic materials 0.000 claims abstract description 25
- 239000002253 acid Substances 0.000 claims abstract description 20
- 239000003599 detergent Substances 0.000 claims abstract description 20
- 229910052767 actinium Inorganic materials 0.000 claims abstract description 17
- QQINRWTZWGJFDB-UHFFFAOYSA-N actinium atom Chemical compound [Ac] QQINRWTZWGJFDB-UHFFFAOYSA-N 0.000 claims abstract description 17
- FZLIPJUXYLNCLC-UHFFFAOYSA-N lanthanum atom Chemical compound [La] FZLIPJUXYLNCLC-UHFFFAOYSA-N 0.000 claims abstract description 17
- 239000007791 liquid phase Substances 0.000 claims abstract description 9
- 238000000746 purification Methods 0.000 claims abstract description 9
- 230000001105 regulatory effect Effects 0.000 claims abstract description 4
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 claims description 33
- 229910017604 nitric acid Inorganic materials 0.000 claims description 33
- 239000000243 solution Substances 0.000 claims description 27
- 238000002156 mixing Methods 0.000 claims description 25
- MUBZPKHOEPUJKR-UHFFFAOYSA-N Oxalic acid Chemical compound OC(=O)C(O)=O MUBZPKHOEPUJKR-UHFFFAOYSA-N 0.000 claims description 21
- WCRZEXKDNPAXKW-UHFFFAOYSA-N [La].[Ac] Chemical compound [La].[Ac] WCRZEXKDNPAXKW-UHFFFAOYSA-N 0.000 claims description 19
- 238000000926 separation method Methods 0.000 claims description 16
- STCOOQWBFONSKY-UHFFFAOYSA-N tributyl phosphate Chemical compound CCCCOP(=O)(OCCCC)OCCCC STCOOQWBFONSKY-UHFFFAOYSA-N 0.000 claims description 14
- URDCARMUOSMFFI-UHFFFAOYSA-N 2-[2-[bis(carboxymethyl)amino]ethyl-(2-hydroxyethyl)amino]acetic acid Chemical compound OCCN(CC(O)=O)CCN(CC(O)=O)CC(O)=O URDCARMUOSMFFI-UHFFFAOYSA-N 0.000 claims description 8
- 239000011259 mixed solution Substances 0.000 claims description 8
- 239000000203 mixture Substances 0.000 claims description 8
- 239000003350 kerosene Substances 0.000 claims description 7
- 235000006408 oxalic acid Nutrition 0.000 claims description 7
- 238000000658 coextraction Methods 0.000 claims description 6
- BWSRLMFHGZNSGI-UHFFFAOYSA-N 2-[3-[6-[5,6-bis(2-sulfophenyl)-1,2,4-triazin-3-yl]pyridin-2-yl]-6-(2-sulfophenyl)-1,2,4-triazin-5-yl]benzenesulfonic acid Chemical compound OS(=O)(=O)C1=CC=CC=C1C1=NN=C(C=2N=C(C=CC=2)C=2N=C(C(C=3C(=CC=CC=3)S(O)(=O)=O)=NN=2)C=2C(=CC=CC=2)S(O)(=O)=O)N=C1C1=CC=CC=C1S(O)(=O)=O BWSRLMFHGZNSGI-UHFFFAOYSA-N 0.000 claims description 3
- WCAFTTMKCJEYAI-UHFFFAOYSA-N 2-ethoxy-2-hexyl-n,n'-dimethyl-n,n'-dioctylpropanediamide Chemical compound CCCCCCCCN(C)C(=O)C(CCCCCC)(OCC)C(=O)N(C)CCCCCCCC WCAFTTMKCJEYAI-UHFFFAOYSA-N 0.000 claims description 3
- 238000001704 evaporation Methods 0.000 claims description 3
- 230000008020 evaporation Effects 0.000 claims description 3
- 238000009501 film coating Methods 0.000 claims description 2
- 239000007888 film coating Substances 0.000 claims description 2
- 239000000047 product Substances 0.000 abstract description 45
- 239000012467 final product Substances 0.000 abstract description 3
- 230000003647 oxidation Effects 0.000 abstract description 3
- 238000007254 oxidation reaction Methods 0.000 abstract description 3
- 229910052685 Curium Inorganic materials 0.000 description 22
- 239000002927 high level radioactive waste Substances 0.000 description 19
- 229910052747 lanthanoid Inorganic materials 0.000 description 19
- 150000002602 lanthanoids Chemical class 0.000 description 19
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 15
- 238000011282 treatment Methods 0.000 description 12
- 239000003153 chemical reaction reagent Substances 0.000 description 8
- VRZYWIAVUGQHKB-UHFFFAOYSA-N 2-[2-(dioctylamino)-2-oxoethoxy]-n,n-dioctylacetamide Chemical compound CCCCCCCCN(CCCCCCCC)C(=O)COCC(=O)N(CCCCCCCC)CCCCCCCC VRZYWIAVUGQHKB-UHFFFAOYSA-N 0.000 description 7
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 7
- 229910021645 metal ion Inorganic materials 0.000 description 7
- 230000002285 radioactive effect Effects 0.000 description 6
- 229910052772 Samarium Inorganic materials 0.000 description 5
- 239000008139 complexing agent Substances 0.000 description 5
- 239000002915 spent fuel radioactive waste Substances 0.000 description 5
- 229910052693 Europium Inorganic materials 0.000 description 4
- 229910052688 Gadolinium Inorganic materials 0.000 description 4
- 238000004458 analytical method Methods 0.000 description 4
- 230000000052 comparative effect Effects 0.000 description 4
- 239000012043 crude product Substances 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- KZUNJOHGWZRPMI-UHFFFAOYSA-N samarium atom Chemical compound [Sm] KZUNJOHGWZRPMI-UHFFFAOYSA-N 0.000 description 4
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 3
- 206010041662 Splinter Diseases 0.000 description 3
- OGPBJKLSAFTDLK-UHFFFAOYSA-N europium atom Chemical compound [Eu] OGPBJKLSAFTDLK-UHFFFAOYSA-N 0.000 description 3
- UIWYJDYFSGRHKR-UHFFFAOYSA-N gadolinium atom Chemical compound [Gd] UIWYJDYFSGRHKR-UHFFFAOYSA-N 0.000 description 3
- 238000002354 inductively-coupled plasma atomic emission spectroscopy Methods 0.000 description 3
- 229910052750 molybdenum Inorganic materials 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 229910052712 strontium Inorganic materials 0.000 description 3
- CIOAGBVUUVVLOB-UHFFFAOYSA-N strontium atom Chemical compound [Sr] CIOAGBVUUVVLOB-UHFFFAOYSA-N 0.000 description 3
- 238000012360 testing method Methods 0.000 description 3
- 229910052727 yttrium Inorganic materials 0.000 description 3
- 229910052684 Cerium Inorganic materials 0.000 description 2
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 description 2
- 229910052779 Neodymium Inorganic materials 0.000 description 2
- 229910052781 Neptunium Inorganic materials 0.000 description 2
- 229910052778 Plutonium Inorganic materials 0.000 description 2
- 229910052777 Praseodymium Inorganic materials 0.000 description 2
- CIOAGBVUUVVLOB-NJFSPNSNSA-N Strontium-90 Chemical compound [90Sr] CIOAGBVUUVVLOB-NJFSPNSNSA-N 0.000 description 2
- 229910052770 Uranium Inorganic materials 0.000 description 2
- 229910052790 beryllium Inorganic materials 0.000 description 2
- GWXLDORMOJMVQZ-UHFFFAOYSA-N cerium Chemical compound [Ce] GWXLDORMOJMVQZ-UHFFFAOYSA-N 0.000 description 2
- TVFDJXOCXUVLDH-RNFDNDRNSA-N cesium-137 Chemical compound [137Cs] TVFDJXOCXUVLDH-RNFDNDRNSA-N 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000009616 inductively coupled plasma Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 230000000873 masking effect Effects 0.000 description 2
- 239000012528 membrane Substances 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 239000011733 molybdenum Substances 0.000 description 2
- QEFYFXOXNSNQGX-UHFFFAOYSA-N neodymium atom Chemical compound [Nd] QEFYFXOXNSNQGX-UHFFFAOYSA-N 0.000 description 2
- LFNLGNPSGWYGGD-UHFFFAOYSA-N neptunium atom Chemical compound [Np] LFNLGNPSGWYGGD-UHFFFAOYSA-N 0.000 description 2
- 229910052763 palladium Inorganic materials 0.000 description 2
- OYEHPCDNVJXUIW-UHFFFAOYSA-N plutonium atom Chemical compound [Pu] OYEHPCDNVJXUIW-UHFFFAOYSA-N 0.000 description 2
- PUDIUYLPXJFUGB-UHFFFAOYSA-N praseodymium atom Chemical compound [Pr] PUDIUYLPXJFUGB-UHFFFAOYSA-N 0.000 description 2
- VSZWPYCFIRKVQL-UHFFFAOYSA-N selanylidenegallium;selenium Chemical compound [Se].[Se]=[Ga].[Se]=[Ga] VSZWPYCFIRKVQL-UHFFFAOYSA-N 0.000 description 2
- 238000001228 spectrum Methods 0.000 description 2
- JFALSRSLKYAFGM-UHFFFAOYSA-N uranium(0) Chemical compound [U] JFALSRSLKYAFGM-UHFFFAOYSA-N 0.000 description 2
- VWQVUPCCIRVNHF-UHFFFAOYSA-N yttrium atom Chemical compound [Y] VWQVUPCCIRVNHF-UHFFFAOYSA-N 0.000 description 2
- 102100032373 Coiled-coil domain-containing protein 85B Human genes 0.000 description 1
- FCKYPQBAHLOOJQ-UHFFFAOYSA-N Cyclohexane-1,2-diaminetetraacetic acid Chemical compound OC(=O)CN(CC(O)=O)C1CCCCC1N(CC(O)=O)CC(O)=O FCKYPQBAHLOOJQ-UHFFFAOYSA-N 0.000 description 1
- 101000868814 Homo sapiens Coiled-coil domain-containing protein 85B Proteins 0.000 description 1
- 102100040653 Tryptophan 2,3-dioxygenase Human genes 0.000 description 1
- 101710136122 Tryptophan 2,3-dioxygenase Proteins 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 230000003321 amplification Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000005255 beta decay Effects 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 230000003750 conditioning effect Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 230000029087 digestion Effects 0.000 description 1
- LVTYICIALWPMFW-UHFFFAOYSA-N diisopropanolamine Chemical compound CC(O)CNCC(C)O LVTYICIALWPMFW-UHFFFAOYSA-N 0.000 description 1
- 239000003085 diluting agent Substances 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000012634 fragment Substances 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- 239000003446 ligand Substances 0.000 description 1
- 238000000622 liquid--liquid extraction Methods 0.000 description 1
- WRIRWRKPLXCTFD-UHFFFAOYSA-N malonamide Chemical compound NC(=O)CC(N)=O WRIRWRKPLXCTFD-UHFFFAOYSA-N 0.000 description 1
- 239000003758 nuclear fuel Substances 0.000 description 1
- 238000003199 nucleic acid amplification method Methods 0.000 description 1
- 230000010355 oscillation Effects 0.000 description 1
- 230000001151 other effect Effects 0.000 description 1
- 238000005191 phase separation Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000005201 scrubbing Methods 0.000 description 1
- 230000035945 sensitivity Effects 0.000 description 1
- 238000000638 solvent extraction Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 229910052726 zirconium Inorganic materials 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
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- Extraction Or Liquid Replacement (AREA)
Abstract
The invention relates to a method for extracting and separating minor actinides by using a strontium americium recovery process, which comprises the following steps of: extracting lanthanum and actinium, extracting an extractant organic phase and a feed liquid aqueous phase to obtain americium-first load organic phase; lanthanum and actinium purification, washing a detergent water phase and an americium-first loaded organic phase to obtain an americium-second loaded organic phase; back-extracting lanthanum and actinium, and back-extracting aqueous phase of back-extracting agent and second load organic phase of americium to obtain liquid-water phase of product; americium two cycles: concentrating lanthanum and actinium for regulating acid, and concentrating and regulating acid to obtain a concentrated product liquid phase; extracting lanthanum and actinium, extracting an extracting agent organic phase and a concentrated product liquid-water phase to obtain a second first load organic phase of americium; purifying lanthanum and actinium, and washing the aqueous phase of the detergent and the second first loaded organic phase of the americium to obtain the second loaded organic phase of the americium; and separating lanthanum from actinium, and carrying out reverse extraction on the aqueous phase of the stripping agent and the second load of americium to obtain a liquid-water phase of the product. Compared with the prior art, the invention does not involve oxidation and pH level acid regulation; the process has high lanthanum and actinium separating factor and high purity of final product.
Description
Technical Field
The invention belongs to the technical fields of nuclear chemical industry and spent fuel post-treatment, and relates to a method for extracting and separating minor actinides by using a strontium americium recovery process.
Background
In the post-treatment process of spent fuel, a large amount of high-level waste liquid can be generated through the PUREX flow, and the treatment of the high-level waste liquid is a key ring for restricting the nuclear fuel circulation. The minor actinides such as americium (Am) and curium (Cm) are the most important sources of alpha radioactivity in the high level waste liquid, and studies have shown that if the high level waste liquid is not subjected to any separation treatment, the minor actinides therein have a last ten thousand years effect on the environment, and if the minor actinides therein are separated, the time of the effect of the high level waste liquid on the environment is reduced from last ten thousand years to hundreds of years. In addition, minor actinides are alpha-radioactive, and the presence of alpha-radioactive releases a significant amount of decay heat, which results in the inability of the high level waste to be directly subjected to solidified geologic treatments. Therefore, the separation and extraction of americium, curium and other minor actinides in the high-level radioactive waste liquid has great ecological significance.
Americium, curium and other minor actinides are also important heavy metal resources, and their alpha radioactivity can be used as an important raw material for alpha radioactive sources and as an important raw material for (alpha, n) neutron sources, such as americium-beryllium neutron sources, curium-beryllium neutron sources and the like. In addition, during the production of nuclides, nuclides with close atomic numbers can be generally put into a reactor for irradiation, and nuclear products with higher atomic numbers are obtained through a series of neutron absorption and beta decay, so that nuclides such as americium, curium and the like can be used as raw materials for the production of actinide nuclides with higher atomic numbers, and have great economic values.
The international proposal is about the process method for separating and extracting americium, curium and other minor actinides from high-level radioactive waste liquid, such as the TRPHEAX process in the United states, the DIMAEX process in France, the DIPA process in Japan and the TRPO process of the national university of Qinghua, which are all verified by thermal experiments and can realize the separation of lanthanum and actinides to a certain extent, but have a plurality of problems, such as high stripping difficulty, sensitivity to acidity and the like.
Patent CN109750164a discloses a method for selectively extracting and separating trivalent actinides and lanthanides in spent fuel post-treatment, which uses ntaamid (n-Oct) as an extractant, kerosene as a diluent, water-soluble ligand TEE-BisDGA as a detergent, a hydroxycarboxylic complexing agent or an aminocarboxylic complexing agent or nitric acid solution as a stripping agent, and a multistage extraction process is used to extract a large amount of actinides and part of lanthanides from a feed liquid, then the lanthanides in a loaded organic phase are removed by using the detergent, and finally the actinides are stripped from the organic phase by using the stripping agent. However, this patent introduces more new reagents during the washing stage, and in the course of the actual post-treatment, great care is required to introduce new reagents, the safety of which must be adequately assessed; furthermore, the stripping stage in this patent requires an acid conditioning of the stripping system concerned in the ph=3.5-5.5 range, which is essentially impossible to achieve in practical applications.
Patent CN109234534a discloses a process for co-extracting trivalent actinides and trivalent lanthanides from high level radioactive waste liquid by extracting trivalent actinides and trivalent lanthanides into an organic phase in a 1A tank using an extraction system, a washing system and washing Zr, pd and other split elements; and back-extracting the trivalent actinides and trivalent lanthanides by using a back-extraction system. However, the patent needs to regulate the acid of the source of the high-level waste liquid, the nitric acid concentration in the source of the high-level waste liquid is about 3mol/L, and the nitric acid concentration in the source of the high-level waste liquid needs to be increased to 4-4.5mol/L, so that the complexity of the process is increased.
Disclosure of Invention
The invention aims to overcome at least one defect of the prior art and provide a method for extracting and separating minor actinides by using a strontium americium recovery process, which has very fast extraction and back extraction kinetics processes and does not involve special operations such as oxidation, pH level acid regulation and the like in the implementation process; the lanthanoid actinium separation factor of the process is high, and the purity of the final product is high.
The aim of the invention can be achieved by the following technical scheme:
one of the technical schemes of the invention is to provide a method for extracting and separating minor actinides by using a strontium americium recovery process, which comprises the following steps:
(1) Americium one cycle:
(1-1) lanthanum actinium co-extraction:
mixing and oscillating an extractant organic phase and a feed liquid water phase, standing, extracting (Extraction) to obtain an americium-first loaded organic phase and an Extraction raffinate water phase, taking the Extraction raffinate water phase out as a source item of a strontium Extraction process after two phases are thoroughly separated, and separating the Extraction raffinate water phase to obtain the americium-first loaded organic phase, wherein in the step, the Extraction rate of americium (Am), curium (Cm) and other minor actinides and lanthanide nuclides is high, the americium-first loaded organic phase has part of splinter product nuclides except for the lanthanides and the externally irradiated radionuclide is left in the Extraction raffinate water phase;
(1-2) lanthanum actinium purification:
the method comprises the steps of mixing and oscillating a detergent water phase and an americium-first loaded organic phase, standing, washing (Scrubbing) to obtain an americium-second loaded organic phase and a washing liquid water phase, removing the washing liquid water phase after the two phases are thoroughly separated, and separating the washing liquid water phase to obtain the americium-second loaded organic phase, wherein the step is mainly used for washing and removing split product nuclides in the americium-first loaded organic phase, and a small amount of externally irradiated radionuclides, and in addition, a considerable part of light lanthanum actinides in the americium-first loaded organic phase can be washed and removed, the loss rate of target minor actinides is low, and the other effect of the step is to adjust the acidity in the americium-first loaded organic phase and provide a proper acidity environment for the subsequent back extraction of the target minor actinides;
(1-3) lanthanum actinium stripping:
the method comprises the steps of mixing and oscillating a Stripping agent aqueous phase with an americium-second loaded organic phase, standing, carrying out back extraction (Stripping) to obtain a first product liquid aqueous phase and a poor organic phase, recovering the first product liquid aqueous phase after the two phases are thoroughly separated, and returning the poor organic phase to a step (1-1) after alkaline washing and acid washing purification, wherein the step is mainly used for obtaining a target minor actinide crude product in the americium-second loaded organic phase, and the steps (1-1) to (1-3) can be used for greatly purifying the target minor actinide product in the organic phase, so that the recovery of the target minor actinide product such as americium, curium and the like can be realized, the purity of the target minor actinide product is high, and the gamma radioactivity of a crude product liquid can be greatly reduced relative to a source item;
(2) Americium two cycles:
(2-1) concentration and acid adjustment of lanthanum and actinium product liquid:
concentrating the first product liquid phase to obtain a concentrated product liquid phase, and regulating acidity;
(2-2) lanthanum actinium co-extraction:
mixing and oscillating an extractant organic phase and a concentrated product liquid-water phase, standing, extracting to obtain an americium second first-load organic phase and a raffinate water phase, removing the raffinate water phase after the two phases are thoroughly separated, separating the raffinate water phase to obtain an americium second first-load organic phase, wherein a large amount of target minor actinides americium, curium and the like enter the americium second first-load organic phase, and enter the americium second first-load organic phase along with americium and curium and lanthanide nuclides;
(2-3) lanthanum actinium purification:
mixing and oscillating a detergent aqueous phase and an americium second first-loaded organic phase, standing, washing to obtain an americium second-loaded organic phase and a washing liquid aqueous phase, removing the washing liquid aqueous phase after the two phases are thoroughly separated, and separating the washing liquid aqueous phase to obtain an americium second-loaded organic phase, wherein light lanthanum actinides such as lanthanum (La), cerium (Ce), praseodymium (Pr), neodymium (Nd), samarium (Sm) and the like in the americium second-loaded organic phase enter the washing liquid aqueous phase through the step, a small amount of uranium (U), plutonium (Pu) and neptunium (Np) in the americium second-loaded organic phase also enter the washing liquid aqueous phase, and lanthanum actinides such as europium (Eu), gadolinium (Gd) and the like and a small amount of samarium, americium and curium and the like remain in the americium second-loaded organic phase for further treatment;
(2-4) lanthanum actinium separation:
the aqueous phase of the stripping agent and the second loaded organic phase of the americium are mixed and oscillated, and are stood and subjected to back extraction to obtain a second product liquid phase and a lean organic phase, the lean organic phase is removed after the two phases are thoroughly separated, the lean organic phase is separated to obtain a second product liquid phase, at the moment, the americium and curium in the second loaded organic phase carry out the second product liquid phase, and lanthanide elements such as europium, gadolinium, samarium and the like in the second loaded organic phase of the americium are continuously remained in the lean organic phase, thereby realizing the separation of target minor actinides such as americium, curium and the like from lanthanide, and realizing the high-efficiency separation of the americium, curium and lanthanide nuclides through the back extraction of the separation of lanthanum and actinide in total two cycles.
Further, in the step (1-1), the organic phase of the extractant is a kerosene (TPH) mixture of a separating agent and tributyl phosphate (TBP), wherein the separating agent comprises N, N, N ', N' -tetraoctyl-3-oxaglutaramide (TODGA), N, N '-dimethyl-N, N' -dioctyl-hexylethoxy malonamide (DMDOHEMA) or N, N '-dimethyl-N, N' -dibutyl-hexylethoxy malonamide (DMDOHEMA), the concentration of the separating agent is 0.02-0.2mol/L, the concentration of the tributyl phosphate is 0.1-0.5mol/L, and the volume ratio of the organic phase of the extractant to the aqueous phase of the feed liquid is (1-10): 1.
Further, in the step (2-2), the organic phase of the extractant adopts a kerosene mixture of separating agent and tributyl phosphate, the separating agent comprises N, N, N ', N' -tetraoctyl-3-oxaglutaramide, N, N '-dimethyl-N, N' -dioctyl-hexyl ethoxy malonamide or N, N '-dimethyl-N, N' -dibutyl-hexyl ethoxy malonamide, the concentration of the separating agent is 0.1-0.5mol/L, the concentration of the tributyl phosphate is 0.5-1.5mol/L, and the volume ratio of the organic phase of the extractant to the liquid-water phase of the concentrated product is (1-10): 1.
As a preferable technical scheme, the feed liquid water phase in the step (1-1) adopts high-level waste liquid, the high-level waste liquid is raffinate obtained after the spent fuel solution is subjected to the PUREX process, and the raffinate contains strontium-90% 90 Sr and cesium-137% 137 Cs), and other exotic radionuclides, and other fragment product nuclides such as yttrium (Y), molybdenum (Mo), zirconium (Zr), palladium (Pd), and targeted minor actinide nuclides such as americium, curium, and the like.
Further, the mixing and shaking time in the steps (1-1) and (2-2) is 10-15min, the standing time is 5-10min, the extraction temperature is room temperature, the number of stages is 8-16, and the form comprises countercurrent or cross flow.
Further, the aqueous detergent phase in step (1-2) comprises nitric acid (HNO) 3 ) The mixed solution of nitric acid and oxalic acid or the mixed solution of nitric acid and N- (2-hydroxyethyl) ethylenediamine-N, N ', N' -triacetic acid (HEDTA), the acid concentration is 2-4mol/L, and the volume ratio of the aqueous phase of the detergent to the first loaded organic phase of americium is (1-10): 1;
the aqueous phase of the detergent in the step (2-3) comprises a nitric acid solution, a mixed solution of nitric acid and oxalic acid, or a mixed solution of nitric acid and N- (2-hydroxyethyl) ethylenediamine-N, N ', N' -triacetic acid, the acid concentration is 0.5-3mol/L, and the volume ratio of the aqueous phase of the detergent to the first load organic phase of americium is (1-10): 1.
Further, the mixing and shaking time in the steps (1-2) and (2-3) is 10-15min, the standing time is 5-10min, the washing temperature is room temperature, the number of stages is 8-16, and the form comprises countercurrent or cross flow.
Further, the stripping agent water phase in the step (1-3) comprises nitric acid solution or water, the concentration of the nitric acid is 0.01-0.1mol/L, and the volume ratio of the stripping agent water phase to the americium-second load organic phase is (1-10): 1.
Further, the stripping agent aqueous phase in the step (2-4) adopts a separating agent solution and a nitric acid solution, wherein the separating agent comprises 2, 6-bis (5, 6-bis (sulfophenyl) -1,2, 4-triazin-3-yl) pyridine (HSO) 3 -Ph-BTP) or N, N-6,6 '-bis (5, 6-bis (sulfophenyl) -1,2, 4-triazinyl) -2,2' -bipyridine (HSO) 3 -Ph-BTBP), the concentration of the separating agent is 0.01-0.1mol/L, the concentration of nitric acid is 0.5-1.5mol/L, and the volume ratio of the aqueous phase of the stripping agent to the second loaded organic phase of americium is (1-10): 1.
Further, the mixing and oscillating time in the steps (1-3) and (2-4) is 10-15min, the standing time is 5-10min, the back extraction temperature is room temperature, the number of stages is 8-16, and the form comprises countercurrent or cross flow.
As a preferable technical scheme, the alkaline washing reagent in the step (1-3) adopts sodium hydroxide (NaOH) solution, and the concentration of the sodium hydroxide is 1-1.5mol/L;
the acid washing reagent adopts nitric acid solution, and the concentration of the nitric acid is 1-2mol/L;
the flow ratio (A/O) of the alkali wash to the acid wash is 0.1-0.5.
Further, the concentration multiple in the step (2-1) is 30-50 times, the form comprises film coating or evaporation, the reagent for adjusting the acidity adopts nitric acid solution, the concentration of the nitric acid is 10-14mol/L, and the concentration of the acid after adjustment is 0.8-1.2mol/L.
Compared with the prior art, the invention has the following beneficial effects:
(1) The method adopts a kerosene (TPH) mixture of N, N, N ', N' -tetraoctyl-3-oxa-diamide (TODGA) and tributyl phosphate (TBP) in a specific flow ratio to carry out combined extraction on actinides such as americium, curium and the like in high-level waste liquid, and in the prior art, masking agents such as oxalic acid, N-hydroxyethyl ethylenediamine triacetic acid (HEDTA) and the like are additionally added into a source item to complex a split product in the source item in the step, so that the masking agents are not needed, thereby enabling raffinate to be purer to facilitate subsequent treatment, and a complexing agent such as oxalic acid and the like is not allowed to be added into a system in the treatment process of the real high-level waste liquid;
(2) The method adopts one step to wash and purify the loaded organic phase in the second and third steps of the first and second americium cycles, adopts a nitric acid solution in a specific flow ratio mode as the adopted detergent, achieves the purification effect which can be realized only by washing in a plurality of steps in the prior art, and adopts the detergent in the prior art to add complexing agents such as oxalic acid, N-hydroxyethyl ethylenediamine triacetic acid, 1, 2-cyclohexanediamine tetraacetic acid (CDTA) and the like, so that the problems described above can also occur, and the invention abandons the complexing agents to ensure that the whole system is safer to operate;
(3) In the third step of the first cycle and the fourth step of the second cycle of the americium, the specific flow ratio in the specific flow ratio form is adopted to carry out back extraction on the target minor actinides nuclides in the loaded organic phase and multiplexing the organic phase, the organic phase cannot be multiplexed in the prior art, the cost can be greatly saved by multiplexing the organic phase, and the method is very important for industrialization;
(4) The concentration process is adopted to increase the concentration of product nuclides in the first step of americium two-cycle, so that the subsequent lanthanum and actinium separation treatment is facilitated, which is one of the origins of the invention; the americium one cycle and the americium two cycles of the invention not only play roles in extracting target minor actinides, but also play roles in radioactive degradation, and compared with a high-level waste liquid source, the total gamma radioactivity of lanthanum actinium products after the americium one cycle can be reduced by thousands to ten thousands times;
(5) The americium second cycle of the present invention uses, in the fourth step, a specific separation reagent 2, 6-bis (5, 6-bis (sulfophenyl) -1,2, 4-triazin-3-yl) pyridine (HSO) in a specific flow ratio form, hydrophilic, high lanthanum actinide (500-2000) 3 -Ph-BTP) or N, N-6,6 '-bis (5, 6-bis (sulfophenyl) -1,2, 4-triazinyl) -2,2' -bipyridine (HSO) 3 -Ph-BTBP) solution and nitric acid solution, to cause the target minor actinide product to go away from the aqueous phase, which solves the problems of difficult stripping and low kinetics of the target nuclide in the prior art;
(6) The invention can realize the purposes of reducing gamma radioactivity and retaining alpha radioactivity of high-level waste liquid by optimizing and selecting reagents and optimizing and improving the process aiming at the integration of americium, curium and other nuclides extraction and strontium recovery;
(7) The method has simple flow links, does not increase the quantity of the high-level waste liquid, has fast extraction and back extraction kinetics processes, does not involve special operations such as oxidation, pH level acid adjustment and the like in the implementation process, belongs to simple liquid-liquid extraction and back extraction operations, and is easy for industrial amplification;
(8) The lanthanum and actinium separation factor of the process is high, and the purity of the final product is high.
Drawings
Figure 1 is a schematic illustration of a americium-cycle flow diagram of a method for extracting and separating minor actinides from a process for the recovery of strontium americium in an embodiment of the invention;
fig. 2 is a schematic illustration of a americium two cycle flow diagram of a method for extracting and separating minor actinides from a process for the recovery of strontium americium in an embodiment of the invention.
Detailed Description
The present invention will be described in detail with reference to specific examples. The present embodiment is implemented on the premise of the technical scheme of the present invention, and a detailed implementation manner and a specific operation process are given, but the protection scope of the present invention is not limited to the following examples.
The equipment used in the following examples is representative of conventional equipment in the art unless otherwise specified; unless otherwise indicated, all reagents used are commercially available or prepared by methods conventional in the art, and all of the following examples, not specifically described, are accomplished by means of conventional experimentation in the art.
Examples:
a method for extracting and separating minor actinides by using a strontium americium recovery process, as shown in fig. 1 and 2, specifically comprising the following steps:
(1) Americium one cycle:
(1-1) lanthanum actinium co-extraction:
aqueous phase: high-emission waste liquid and spent fuel solution is extracted residual liquid after the PUREX process, and the extracted residual liquid contains strontium-90% 90 Sr and cesium-137% 137 Cs), and other exotic radionuclides, and splinter product nuclides such as yttrium (Y), molybdenum (Mo), zirconium (Zr), palladium (Pd), and targeted minor actinides such as americium (Am), curium (Cm)
Organic phase: kerosene (TPH) mixture of 0.05mol/L N, N, N ', N' -tetraoctyl-3-oxaglutaramide (TODGA) and 0.5mol/L tributyl phosphate (TBP)
The operation is as follows: mixing and oscillating the extractant organic phase and the feed liquid water phase for 15min according to the volume ratio of 1:1, standing for 5min at room temperature, obtaining americium-first loaded organic phase and raffinate water phase through eight-stage countercurrent Extraction (Extraction), taking out the raffinate water phase through a knockout as a source item of a strontium Extraction process after the two phases are thoroughly separated, and obtaining americium-first loaded organic phase after the raffinate water phase is separated, wherein the Extraction rate of americium, curium and other minor actinides and lanthanide nuclides is 99.94%, more than 99.9%, the americium-first loaded organic phase comprises part of splinter product nuclides except lanthanum actinides, such as 99.9% of Y, 20.5% of Mo, 99.4% of Zr, 99.8% of Pd and the like relative to the feed liquid water phase, and the radionuclides such as phases are irradiated outsideFor the feed liquid and water phase 99% 90 Sr、 137 Cs and the like will remain in the raffinate aqueous phase;
(1-2) lanthanum actinium purification:
organic phase: americium-first loaded organic phase obtained in step (1-1)
Aqueous phase: 4mol/L nitric acid (HNO) 3 ) Solution
The operation is as follows: mixing and oscillating the aqueous phase of the detergent and the first loaded organic phase of the americium at a volume ratio of 1.5:1 for 15min, standing for 5min at room temperature to obtain a second loaded organic phase of the americium and a washing liquid aqueous phase by eight-stage countercurrent washing (washing), removing the washing liquid aqueous phase by a liquid separator after the two phases are thoroughly separated, and separating the washing liquid aqueous phase to obtain the second loaded organic phase of the americium, wherein the step is mainly for washing and removing the split product nuclides in the first loaded organic phase of the americium, mainly all Mo, zr and the like, Y, pd and the like are continuously remained in the first loaded organic phase of the americium, and a small amount of externally irradiated radionuclides such as 90 Sr、 137 Cs, etc., and in addition, 60-70% of light lanthanum actinides in the americium-first loaded organic phase, such as 64.7% lanthanum (La), 62.9% cerium (Ce), 69.2% praseodymium (Pr), 63.1% neodymium (Nd), 66.4% samarium (Sm), etc., may be washed and removed, while the loss rate of the target minor actinide americium is 2.6%, not more than 3%, another function of this step is to adjust the acidity in the americium-first loaded organic phase, providing a suitable acidity environment for subsequent stripping of the target minor actinide;
(1-3) lanthanum actinium stripping:
organic phase: americium-second loaded organic phase obtained in step (1-2)
Aqueous phase: 0.01mol/L HNO 3 Solution
The operation is as follows: mixing the aqueous phase of the Stripping agent with the americium-second loaded organic phase in a volume ratio of 3:1, oscillating for 15min, standing for 5min at room temperature, performing eight-stage countercurrent Stripping (Stripping) to obtain a first product aqueous phase and a lean organic phase, recovering the first product aqueous phase by a knockout after the two phases are thoroughly separated, and performing alkaline washing and acid washing (1.2 mol/L sodium hydroxide (NaOH) solution and 1.5mol/L HNO solution on the lean organic phase 3 The solution was purified to have a flow ratio (A/O) of 0.3 and returned to step (1-1), this stepThe method mainly aims at obtaining a target minor actinide crude product in an americium-second loaded organic phase, the target minor actinide product in the organic phase can be greatly purified through the steps (1-1) to (1-3), the recovery of target minor actinide such as Am, cm and the like of 95.7% (more than 90%) can be realized through the step, the purity of the target minor actinide product is 75%, the purity of the target minor actinide product is more than 70%, and the gamma radioactivity of crude product liquid can be reduced by 4 orders of magnitude relative to a source item;
the main purpose of steps (1-1) to (1-3) is the crude extraction of the target minor actinides Am, cm and the reduction of gamma radioactivity;
(2) Americium two cycles:
(2-1) concentration and acid adjustment of lanthanum and actinium product liquid:
the operation is as follows: the concentration of americium in the aqueous phase of the first product obtained in steps (1-3) is 10.2mg/L, the aqueous phase of the first product is concentrated by a membrane or evaporation 30 times to obtain a concentrated aqueous phase of the product, in this example, the aqueous phase of the first product is concentrated by a membrane, the concentration of americium in the aqueous phase of the first product can be increased to 306mg/L, and the acidity of the aqueous phase of the first product is adjusted to 1.0mol/L by 11mol/L nitric acid;
(2-2) lanthanum actinium co-extraction:
aqueous phase: the concentrated product liquid-water phase obtained in the step (2-2)
Organic phase: TPH mixture of 0.4mol/L TODGA and 1mol/L TBP
The operation is as follows: mixing and oscillating an extractant organic phase and a concentrated product liquid phase for 15min according to the volume ratio of 1:1, standing for 5min, obtaining an americium second first loaded organic phase and a raffinate aqueous phase through eight-stage countercurrent extraction at room temperature, removing the raffinate aqueous phase through a knockout after two phases are thoroughly separated, and obtaining the americium second first loaded organic phase after the raffinate aqueous phase is separated, wherein 98.3 percent and 98.6 percent (more than 98 percent) of target minor actinides Am, cm and the like enter the americium second first loaded organic phase, and enter the americium second first loaded organic phase along with the Am and Cm and also enter a lanthanide;
(2-3) lanthanum actinium purification:
organic phase: americium second first loaded organic phase obtained in step (2-2)
Aqueous phase: 0.5mol/L HNO 3 Solution
The operation is as follows: the method comprises the steps of mixing a detergent aqueous phase with an americium second first-load organic phase in a volume ratio of 1.5:1, oscillating for 15min, standing for 5min, obtaining an americium second-load organic phase and a washing liquid aqueous phase through eight-stage countercurrent washing, removing the washing liquid aqueous phase through a knockout device after the two phases are thoroughly separated, obtaining an americium second-load organic phase after the washing liquid aqueous phase is separated, wherein 60.3% of La, 63.6% of Ce, 65.2% of Pr, 68.5% of Nd, 66.9% of Sm and other 60-70% of light lanthanum actinides in the americium second-load organic phase enter the washing liquid aqueous phase through the step, 11.2% of uranium (U), 13.4% of plutonium (Pu) and 12.7% of neptunium (Np) in the washing liquid aqueous phase also enter the washing liquid aqueous phase, and a small amount of lanthanum actinides such as europium (Eu), gadolinium (Gd) and other as well as small amounts of Sm, am, cm and other actinides can remain in the second-load organic phase for carrying out the treatment for the step of 8.4% and other than 2% of actinium, and other actinium species, and the actinium is not lost for the step of carrying out the second-load phase of 2.4%;
(2-4) lanthanum actinium separation:
organic phase: americium second loaded organic phase obtained in step (2-3)
Aqueous phase: 0.02 mol/L2, 6-bis (5, 6-bis (sulfophenyl) -1,2, 4-triazin-3-yl) pyridine (HSO 3 -Ph-BTP) solution and 1mol/L HNO 3 Solution
The operation is as follows: the aqueous phase of the stripping agent and the second loaded organic phase of the americium are mixed and oscillated for 15min according to the volume ratio of 1:1, the mixture is stood for 5min, the temperature is room temperature, the second product aqueous phase and the poor organic phase are obtained through eight-stage countercurrent stripping, the poor organic phase is removed through a knockout device after the two phases are thoroughly separated, the second product aqueous phase is obtained after the poor organic phase is separated, at the moment, 99.9 percent (more than 99 percent) of Am and Cm of the second loaded organic phase of the americium enter the second product aqueous phase, 99.9 percent of Eu, 99.9 percent of Gd, 99.1 percent of lanthanide elements such as Sm and the like in the second loaded organic phase of the americium are continuously remained in the poor organic phase, thereby realizing the separation of target minor actinides such as Am and Cm from lanthanoids, and 98.4 percent, 98.8 percent (more than 95 percent) of Am and Cm from lanthanoids can be realized through the separation stripping of lanthanoids and actinoid in total two cycles.
The steps of extraction, washing, back extraction and the like relate to mixing oscillation, standing phase separation, liquid separation and the like, wherein a single-stage form can be carried out in a separating funnel and an extraction centrifuge tube and a constant-temperature water bath oscillating table, and a multi-stage countercurrent form can be carried out in a multi-stage full countercurrent mixing clarifying tank and a multi-stage full countercurrent pulse extraction column.
Comparative example:
the method for extracting and separating minor actinides by using strontium americium recovery process is basically the same as the embodiment, and is different in that a single-stage separating funnel and an extraction centrifuge tube are adopted to replace an eight-stage full-countercurrent mixing clarifying tank and a full-countercurrent pulse extraction column by using a constant-temperature water bath oscillating table, and compared with the comparative example, the experimental effect of each step can be greatly improved, and the counter extraction result pairs of main elements in the embodiment and the comparative example are shown in table 1.
Table 1 comparison of the stripping results of the main elements in examples and comparative examples
The non-radioactive metal ion analysis of the data adopts an inductively coupled plasma emission spectrometer (ICP-OES) and an inductively coupled plasma emission mass spectrometer (ICP-MS) to carry out water phase metal ion analysis, and adopts a digestion mode to digest the metal ions in the organic phase, and then uses ICP-OES and ICP-MS to carry out analysis of metal ion concentration.
The radioactive metal ions in the data are analyzed by adopting equipment such as a gamma spectrometer, a beta spectrometer and the like.
The radioactive metal ion analysis step in the data above, hot cell sample preparation-put in gamma spectrometer (test gamma spectrum), put in beta spectrometer (test beta count) -analyze data (nuclide determination by gamma spectrum and beta radioactivity determination by beta count).
The data are used for non-radioactive metal ion test, sample preparation (the sampled feed liquid is diluted into thousands of times, the specific dilution is determined according to the sampled radioactivity), ICP-OES and ICP-MS data analysis-data processing are carried out, and extraction, washing and back extraction efficiency data and target nuclide recovery rate data are obtained.
The previous description of the embodiments is provided to facilitate a person of ordinary skill in the art in order to make and use the present invention. It will be apparent to those skilled in the art that various modifications can be readily made to these embodiments and the generic principles described herein may be applied to other embodiments without the use of the inventive faculty. Therefore, the present invention is not limited to the above-described embodiments, and those skilled in the art, based on the present disclosure, should make improvements and modifications without departing from the scope of the present invention.
Claims (10)
1. A method for extracting and separating minor actinides by using a strontium americium recovery process, which is characterized by comprising the following steps:
(1) Americium one cycle:
(1-1) lanthanum actinium co-extraction:
mixing and oscillating the extractant organic phase and the feed liquid water phase, standing, and extracting to obtain americium-first loaded organic phase and raffinate water phase;
(1-2) lanthanum actinium purification:
mixing and oscillating the aqueous phase of the detergent and the first loaded organic phase of the americium, standing and washing to obtain the second loaded organic phase of the americium and the aqueous phase of the washing liquid;
(1-3) lanthanum actinium stripping:
mixing and oscillating the aqueous phase of the stripping agent and the americium-second loaded organic phase, standing, carrying out stripping to obtain a first product aqueous phase and a lean organic phase, recovering the first product aqueous phase after the two phases are thoroughly separated, and returning the lean organic phase to the step (1-1);
(2) Americium two cycles:
(2-1) concentration and acid adjustment of lanthanum and actinium product liquid:
concentrating the first product liquid phase to obtain a concentrated product liquid phase, and regulating acidity;
(2-2) lanthanum actinium co-extraction:
mixing and oscillating the extractant organic phase and the concentrated product liquid-water phase, standing, and extracting to obtain americium second first loaded organic phase and raffinate water phase;
(2-3) lanthanum actinium purification:
mixing and oscillating the aqueous phase of the detergent with the second first loaded organic phase of the americium, standing and washing to obtain the second loaded organic phase of the americium and a washing liquid aqueous phase;
(2-4) lanthanum actinium separation:
mixing and oscillating the aqueous phase of the stripping agent with the second loaded organic phase of americium, standing, and stripping to obtain a second product aqueous phase and a lean organic phase.
2. The method for separating minor actinides by extraction according to claim 1, wherein in step (1-1), the organic phase of the extractant is a kerosene mixture of separating agent and tributyl phosphate, the separating agent comprises N, N, N ', N' -tetraoctyl-3-oxoglutarate, N, N '-dimethyl-N, N' -dioctyl-hexylethoxymalonamide or N, N '-dimethyl-N, N' -dibutyl-hexylethoxymalonamide, the concentration of the separating agent is 0.02-0.2mol/L, the concentration of tributyl phosphate is 0.1-0.5mol/L, and the volume ratio of the organic phase of the extractant to the aqueous phase of the feed liquid is (1-10): 1.
3. The method according to claim 1, wherein the organic phase of the extractant in step (2-2) is a kerosene mixture of separating agent and tributyl phosphate, the separating agent comprises N, N ' -tetraoctyl-3-oxaglutaramide, N ' -dimethyl-N, N ' -dioctyl-hexylethoxymalonamide or N, N ' -dimethyl-N, N ' -dibutyl-hexylethoxymalonamide, the concentration of separating agent is 0.1-0.5mol/L, the concentration of tributyl phosphate is 0.5-1.5mol/L, and the volume ratio of the organic phase of the extractant to the aqueous phase of the concentrated product is (1-10): 1.
4. The method for separating minor actinides from a strontium americium recovery process according to claim 1, wherein the time of mixing and shaking in steps (1-1) and (2-2) is 10-15min, the time of standing is 5-10min, the temperature of extraction is room temperature, the number of stages is 8-16, and the form comprises countercurrent or cross-current.
5. The method for separating minor actinides from a strontium americium recovery process according to claim 1, wherein in step (1-2), the aqueous phase of the detergent comprises a nitric acid solution, a mixed solution of nitric acid and oxalic acid, or a mixed solution of nitric acid and N- (2-hydroxyethyl) ethylenediamine-N, N' -triacetic acid, the acid concentration is 2-4mol/L, and the volume ratio of the aqueous phase of the detergent to the first loaded organic phase of americium is (1-10): 1;
the aqueous phase of the detergent in the step (2-3) comprises a nitric acid solution, a mixed solution of nitric acid and oxalic acid, or a mixed solution of nitric acid and N- (2-hydroxyethyl) ethylenediamine-N, N ', N' -triacetic acid, the acid concentration is 0.5-3mol/L, and the volume ratio of the aqueous phase of the detergent to the first load organic phase of americium is (1-10): 1.
6. The method for separating minor actinides from a strontium americium recovery process according to claim 1, wherein the time of mixing and shaking in steps (1-2) and (2-3) is 10-15min, the time of standing is 5-10min, the temperature of washing is room temperature, the number of stages is 8-16, and the form comprises countercurrent or cross-current.
7. The method for separating minor actinides from a strontium americium recovery process according to claim 1, wherein the aqueous phase of the stripping agent in step (1-3) comprises nitric acid solution or water, the concentration of nitric acid is 0.01-0.1mol/L, and the volume ratio of the aqueous phase of the stripping agent to the americium-second loaded organic phase is (1-10): 1.
8. The method for separating minor actinides by extraction according to claim 1, wherein the aqueous stripping agent phase in step (2-4) is a solution of a separating agent and a solution of nitric acid, the separating agent comprises 2, 6-bis (5, 6-bis (sulfophenyl) -1,2, 4-triazin-3-yl) pyridine or N, N-6,6 '-bis (5, 6-bis (sulfophenyl) -1,2, 4-triazinyl) -2,2' -bipyridine, the concentration of the separating agent is 0.01-0.1mol/L, the concentration of nitric acid is 0.5-1.5mol/L, and the volume ratio of aqueous stripping agent phase to second load organic phase of americium is (1-10): 1.
9. The method for separating minor actinides by extraction according to claim 1, wherein the time of mixing and shaking in steps (1-3) and (2-4) is 10-15min, the time of standing is 5-10min, the temperature of back extraction is room temperature, the number of stages is 8-16, and the form comprises countercurrent or cross-current.
10. The method for extracting and separating minor actinides from a process for recovering strontium americium according to claim 1, wherein the concentration in step (2-1) is 30-50 times, the form includes film coating or evaporation, the agent for adjusting acidity adopts nitric acid solution, the concentration of nitric acid is 10-14mol/L, and the concentration of acid after adjustment is 0.8-1.2mol/L.
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