CN115874071A - Method for efficiently purifying uranium from iron-boron-uranium-containing bulk concentrate - Google Patents
Method for efficiently purifying uranium from iron-boron-uranium-containing bulk concentrate Download PDFInfo
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- 229910052770 Uranium Inorganic materials 0.000 title claims abstract description 136
- JFALSRSLKYAFGM-UHFFFAOYSA-N uranium(0) Chemical compound [U] JFALSRSLKYAFGM-UHFFFAOYSA-N 0.000 title claims abstract description 128
- 238000000034 method Methods 0.000 title claims abstract description 67
- 239000012141 concentrate Substances 0.000 title claims abstract description 45
- IIQDUMDFXUUECR-UHFFFAOYSA-N [B].[Fe].[U] Chemical compound [B].[Fe].[U] IIQDUMDFXUUECR-UHFFFAOYSA-N 0.000 title claims abstract description 17
- 238000002386 leaching Methods 0.000 claims abstract description 76
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims abstract description 52
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 37
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 37
- 239000001301 oxygen Substances 0.000 claims abstract description 37
- 230000008569 process Effects 0.000 claims abstract description 36
- 238000007731 hot pressing Methods 0.000 claims abstract description 24
- 239000007788 liquid Substances 0.000 claims abstract description 20
- 238000009854 hydrometallurgy Methods 0.000 claims abstract description 15
- ZDVYABSQRRRIOJ-UHFFFAOYSA-N boron;iron Chemical compound [Fe]#B ZDVYABSQRRRIOJ-UHFFFAOYSA-N 0.000 claims abstract description 14
- 238000000926 separation method Methods 0.000 claims abstract description 12
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 9
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 65
- 229910052742 iron Inorganic materials 0.000 claims description 34
- 239000000243 solution Substances 0.000 claims description 30
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 24
- ZOXJGFHDIHLPTG-UHFFFAOYSA-N Boron Chemical compound [B] ZOXJGFHDIHLPTG-UHFFFAOYSA-N 0.000 claims description 14
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims description 14
- 229910052796 boron Inorganic materials 0.000 claims description 14
- 238000001556 precipitation Methods 0.000 claims description 9
- 239000007787 solid Substances 0.000 claims description 9
- 238000005342 ion exchange Methods 0.000 claims description 8
- 235000011121 sodium hydroxide Nutrition 0.000 claims description 8
- 239000011780 sodium chloride Substances 0.000 claims description 7
- 230000001376 precipitating effect Effects 0.000 claims description 5
- 239000003957 anion exchange resin Substances 0.000 claims description 4
- 239000011259 mixed solution Substances 0.000 claims description 4
- 239000002245 particle Substances 0.000 claims description 4
- 238000001179 sorption measurement Methods 0.000 claims description 4
- 238000010828 elution Methods 0.000 claims description 3
- 239000003480 eluent Substances 0.000 claims description 2
- 238000011084 recovery Methods 0.000 abstract description 10
- 239000002910 solid waste Substances 0.000 abstract description 8
- 239000002699 waste material Substances 0.000 abstract description 7
- 230000002285 radioactive effect Effects 0.000 description 14
- 229910052500 inorganic mineral Inorganic materials 0.000 description 8
- 239000011707 mineral Substances 0.000 description 8
- 235000010755 mineral Nutrition 0.000 description 8
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 description 5
- 238000009826 distribution Methods 0.000 description 5
- 239000003456 ion exchange resin Substances 0.000 description 5
- 229920003303 ion-exchange polymer Polymers 0.000 description 5
- 238000006243 chemical reaction Methods 0.000 description 4
- -1 iron ions Chemical class 0.000 description 4
- SZVJSHCCFOBDDC-UHFFFAOYSA-N iron(II,III) oxide Inorganic materials O=[Fe]O[Fe]O[Fe]=O SZVJSHCCFOBDDC-UHFFFAOYSA-N 0.000 description 4
- 238000012545 processing Methods 0.000 description 4
- 238000011161 development Methods 0.000 description 3
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 2
- QVXXDVNZFIFEKW-UHFFFAOYSA-N boranylidyneuranium Chemical compound [U]#B QVXXDVNZFIFEKW-UHFFFAOYSA-N 0.000 description 2
- 238000003912 environmental pollution Methods 0.000 description 2
- 150000002500 ions Chemical class 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 229910021645 metal ion Inorganic materials 0.000 description 2
- 238000005065 mining Methods 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 230000001590 oxidative effect Effects 0.000 description 2
- 229910052683 pyrite Inorganic materials 0.000 description 2
- NIFIFKQPDTWWGU-UHFFFAOYSA-N pyrite Chemical compound [Fe+2].[S-][S-] NIFIFKQPDTWWGU-UHFFFAOYSA-N 0.000 description 2
- 239000011028 pyrite Substances 0.000 description 2
- 229910052952 pyrrhotite Inorganic materials 0.000 description 2
- 238000003904 radioactive pollution Methods 0.000 description 2
- 239000011347 resin Substances 0.000 description 2
- 229920005989 resin Polymers 0.000 description 2
- 239000011435 rock Substances 0.000 description 2
- 239000002893 slag Substances 0.000 description 2
- 238000003723 Smelting Methods 0.000 description 1
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 1
- SGUPDEUNVHKBOH-UHFFFAOYSA-N [Fe].[U] Chemical compound [Fe].[U] SGUPDEUNVHKBOH-UHFFFAOYSA-N 0.000 description 1
- FSHMCSKYTOXLHI-UHFFFAOYSA-G [OH-].[Na+].[U+6].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-] Chemical compound [OH-].[Na+].[U+6].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-] FSHMCSKYTOXLHI-UHFFFAOYSA-G 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 238000004220 aggregation Methods 0.000 description 1
- 230000002776 aggregation Effects 0.000 description 1
- WYTGDNHDOZPMIW-RCBQFDQVSA-N alstonine Natural products C1=CC2=C3C=CC=CC3=NC2=C2N1C[C@H]1[C@H](C)OC=C(C(=O)OC)[C@H]1C2 WYTGDNHDOZPMIW-RCBQFDQVSA-N 0.000 description 1
- 229940037003 alum Drugs 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 229910052598 goethite Inorganic materials 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- AEIXRCIKZIZYPM-UHFFFAOYSA-M hydroxy(oxo)iron Chemical compound [O][Fe]O AEIXRCIKZIZYPM-UHFFFAOYSA-M 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 229910001608 iron mineral Inorganic materials 0.000 description 1
- 239000010808 liquid waste Substances 0.000 description 1
- NUJOXMJBOLGQSY-UHFFFAOYSA-N manganese dioxide Inorganic materials O=[Mn]=O NUJOXMJBOLGQSY-UHFFFAOYSA-N 0.000 description 1
- 238000013508 migration Methods 0.000 description 1
- 230000005012 migration Effects 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 230000002265 prevention Effects 0.000 description 1
- 239000000941 radioactive substance Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 230000000717 retained effect Effects 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 229910000384 uranyl sulfate Inorganic materials 0.000 description 1
Images
Classifications
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- 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
Abstract
The invention provides a method for efficiently purifying uranium from iron-boron-containing uranium bulk concentrate, and relates to the technical field of hydrometallurgy. The invention provides a method for efficiently purifying uranium from iron-boron-containing uranium bulk concentrate, which comprises the following steps: carrying out hot-pressing oxygen leaching on the iron-boron-uranium-containing bulk concentrate, and carrying out solid-liquid separation to obtain uranium-containing leachate and hydrometallurgy tailings; the leaching agent adopted by the hot-pressing oxygen leaching is sulfuric acid solution; the hot-pressing oxygen leaching temperature is 120-145 ℃, the leaching time is 1-6 h, and the oxygen partial pressure is 0.2-1.5 MPa. The method can realize high-efficiency recovery of uranium and reduce the content of radionuclide in solid waste and process waste liquid.
Description
Technical Field
The invention relates to the technical field of hydrometallurgy, in particular to a method for efficiently purifying uranium from iron-boron-uranium mixed concentrate.
Background
The associated radioactive ore is associated with natural radioactive nuclide with a certain specification level besides required mining components, and natural radioactive substances in the associated ore are migrated, enriched and diffused in the processes of mining, smelting, processing and utilizing, and wastes containing natural radioactivity cause radioactive pollution to the environment to a certain extent. The research on the radioactive environmental pollution in the development and utilization processes of the associated mine can provide basic data and scientific basis for the development and utilization of the associated mine and the environmental pollution prevention and control in China. Data show that in the process of developing associated radioactive ore in China, the primary processing is the main source for generating radioactive pollutants, and the radioactive content in raw materials used for deep processing is relatively low. Therefore, radioactive pollution source, scientific development and orderly management are the necessary ways to exert associated resource benefit maximization and improve radioactive environmental protection.
A polymetallic deposit belongs to an associated radioactive mineral resource, the mineral variety in the deposit is various, more than 60 kinds of discovered minerals are present, the mineral substance components are complex, the main useful elements are iron, boron and uranium, the main useful minerals are magnetite, boromagnesite, crystalline uranium ore and boromagnesite, and the secondary useful minerals are pyrrhotite, pyrite and the like. The prior process flow comprises the following steps: the method is characterized in that ore is mined and sorted in the open air to obtain boron-containing iron concentrate, boron concentrate and iron-containing boron-uranium concentrate, radioactive nuclides are mainly concentrated in the iron-containing boron-uranium concentrate in the process, and the radioactive nuclides can be further migrated and diffused in the environment no matter processing recovery or solid waste production, so that the waste liquid and solid waste production in the radioactive nuclide process can be reduced, and radioactive nuclide waste is reduced fundamentally. The method is characterized in that the radionuclide uranium is recovered by adopting hydrometallurgy aiming at boron-iron-containing uranium concentrate, the conventional main process for extracting uranium is low-acid leaching-ion exchange enrichment uranium-sodium hydroxide precipitation uranium, the leaching rate of uranium is 91%, the grade of uranium slag is 0.01%, and the recovery rate of uranium hydrometallurgy is 90%. Residual migration of uranium is mainly focused on three aspects: (1) The crystalline uranium ores are distributed in magnetite ores, magnetite-containing serpentine rocks and magnetite-containing stevensite rocks in a dip-dyed shape, are inserted into associated minerals in a wrapping state, and are closely symbiotic with the iron-containing minerals, so that the leaching difficulty of uranium is increased, and part of uranium cannot be transferred into a solution; (2) In the process of leaching uranium from the uranium ore containing boron and iron, a large amount of iron minerals are dissolved out, so that the capacity of resin for adsorbing uranium is influenced, the resin adsorption efficiency is also influenced, and the recovery rate of uranium is reduced; (3) Part of the iron-containing complex and uranium are adsorbed and eluted by ion exchange resin, a large amount of qualified uranium liquid containing iron ions is directly precipitated to influence the purity of uranium, usually, iron is removed first and then uranium is precipitated, and part of uranium is coprecipitated with iron in the iron removal process. Therefore, the prior art has the problems of low uranium recovery rate and a large amount of radionuclides in solid waste and waste liquid.
Disclosure of Invention
The invention aims to provide a method for efficiently purifying uranium from iron-boron-containing uranium bulk concentrates, which can realize efficient recovery of uranium and reduce the content of radioactive nuclides in solid wastes and process waste liquid.
In order to achieve the above object, the present invention provides the following technical solutions:
the invention provides a method for efficiently purifying uranium from iron-boron-containing uranium bulk concentrate, which comprises the following steps:
carrying out hot-pressing oxygen leaching on the iron-boron-uranium-containing bulk concentrate, and carrying out solid-liquid separation to obtain uranium-containing leachate and hydrometallurgy tailings; the leaching agent adopted by the hot-pressing oxygen leaching is sulfuric acid solution; the hot-pressing oxygen leaching temperature is 120-145 ℃, the leaching time is 1-6 h, and the oxygen partial pressure is 0.2-1.5 MPa.
Preferably, the grade of iron in the mixed concentrate containing iron, boron and uranium is 10-42 wt%, and the grade of uranium is 0.1-0.3 wt%.
Preferably, the mass of the sulfuric acid is 0.5-6% of the mass of the iron-boron-containing uranium bulk concentrate.
Preferably, the liquid-solid ratio of the hot-pressing oxygen leaching is 1-3: 1.
preferably, after obtaining the uranium-bearing leachate, the method further comprises: carrying out ion exchange on the uranium-containing leaching solution to obtain a high-uranium aggregate solution; and precipitating uranium from the high-uranium concentrated solution by using caustic soda flakes or sodium hydroxide particles to obtain a uranium product.
Preferably, the ion exchange comprises: and (3) carrying out an adsorption-leaching process on the uranium-containing leaching solution by adopting strong-base anion exchange resin.
Preferably, the adsorption contact time of the adsorption-leaching process is 3-10 min; the leaching contact time is 30-45 min.
Preferably, the eluting agent adopted in the adsorption-leaching process is a mixed solution of sulfuric acid and sodium chloride.
Preferably, the concentration of the sulfuric acid in the eluting agent is 5-10 g/L; the concentration of the sodium chloride is 50-80 g/L.
Preferably, the temperature of the precipitation is 20-35 ℃; the precipitation time is 3-6 h.
The invention provides a method for efficiently purifying uranium from iron-boron-containing uranium bulk concentrate, which comprises the following steps: carrying out hot-pressing oxygen leaching on the iron-boron-uranium-containing bulk concentrate, and carrying out solid-liquid separation to obtain uranium-containing leachate and hydrometallurgy tailings; the leaching agent adopted by the hot-pressing oxygen leaching is sulfuric acid solution; the hot-pressing oxygen leaching temperature is 120-145 ℃, the leaching time is 1-6 h, and the oxygen partial pressure is 0.2-1.5 MPa. In the hot-pressing oxygen leaching process, uranium reacts with sulfuric acid to generate uranyl sulfate ions which exist in a leaching solution, iron ions dissolved out from the iron-boron-containing uranium bulk concentrate undergo hydrolysis reaction, generated solids such as pyrrhotite and goethite are retained in leaching slag, uranium is leached to the maximum extent to inhibit iron, after solid-liquid separation, the uranium-iron separation efficiency is greatly improved, selective leaching of uranium is realized, and the content of radioactive nuclides in solid waste and process waste liquid is reduced.
In the invention, as the yellow ferric alum is in a crystal shape and has a prismatic smooth physical surface, other element ions cannot be adsorbed and carried, and the loss of valuable metal ions uranium is less; meanwhile, after the leaching process is finished, the viscosity of the slurry can be effectively reduced, and the solid-liquid separation efficiency is accelerated.
Furthermore, the method further enriches uranium through ion exchange and precipitation procedures, and realizes high-efficiency recovery of uranium.
Further, in the hot-pressing oxygen leaching process, after pyrite in the ore is corroded, sulfide is converted into sulfuric acid or sulfate, so that the use amount of sulfuric acid is reduced, and impurity ions in the ore are dissolved out.
The results of the examples show that the method disclosed by the invention is used for extracting uranium from the mixed concentrate containing iron, boron and uranium, the leaching rate of uranium is more than 97%, the comprehensive recovery rate is more than 95%, the concentration of iron in uranium-containing leachate is less than 0.2g/L, and the grade of uranium in hydrometallurgy tailings is reduced to be less than 0.004%.
Drawings
Fig. 1 is a process for the intensified leaching of iron-boron-uranium-containing bulk concentrates according to examples 1-2 of the present invention;
fig. 2 shows the enhanced leaching process of the mixed concentrate containing iron, boron and uranium in embodiments 3 to 4 of the present invention.
Detailed Description
The invention provides a method for efficiently purifying uranium from iron-boron-containing uranium bulk concentrate, which comprises the following steps:
carrying out hot-pressing oxygen leaching on the iron-boron-uranium-containing bulk concentrate, and carrying out solid-liquid separation to obtain uranium-containing leachate and hydrometallurgy tailings; the leaching agent adopted by the hot-pressing oxygen leaching is sulfuric acid solution; the hot-pressing oxygen leaching temperature is 120-145 ℃, the leaching time is 1-6 h, and the oxygen partial pressure is 0.2-1.5 MPa.
In the invention, the grade of iron in the mixed concentrate containing iron, boron and uranium is preferably 10-42 wt%, and more preferably 37.25-41.05 wt%; the grade of uranium is preferably 0.1 to 0.3wt%, more preferably 0.209 to 0.225wt%. In the invention, the particle size of the mixed concentrate containing iron, boron and uranium is preferably-200 meshes, and the proportion is preferably 60-80 wt%. In the invention, the distribution rate of uranium in the mixed iron-boron-containing uranium concentrate (mass content of uranium with 200 meshes in total uranium) is preferably 85-96 wt%, and more preferably 85.2-95.8 wt%.
In the invention, the mass of the sulfuric acid is preferably 0.5-6%, more preferably 1-5% of the mass of the iron-boron-uranium-containing bulk concentrate. In the present invention, the liquid-solid ratio is preferably 1 to 3:1, more preferably 1 to 1.5:1. in the invention, the liquid-solid ratio refers to the mass ratio of the leaching agent to the iron-boron-uranium-containing bulk concentrate.
In the invention, the temperature of the hot-pressing oxygen leaching is preferably 130-140 ℃, the leaching time is preferably 3-5 h, and the oxygen partial pressure is preferably 0.5-0.9 MPa. The method uses oxygen as an oxidant to replace the original pyrolusite, can reduce the introduction of other metal ions, and does not newly add heavy metal components in the solid waste; the dissolved iron ions play a catalytic role in the oxidation process of the crystalline uranium ores during the hot-pressing oxygen leaching process, and the efficiency of oxidizing the crystalline uranium ores by oxygen is accelerated.
After the uranium-bearing leachate is obtained, the method preferably further comprises the following steps: carrying out ion exchange on the uranium-containing leaching solution to obtain a high-uranium aggregation solution; and precipitating uranium from the high-uranium concentrated solution by using caustic soda flakes or sodium hydroxide particles to obtain a uranium product.
In the present invention, the ion exchange preferably comprises: and (3) carrying out an adsorption-leaching process on the uranium-containing leaching solution by adopting strong-base anion exchange resin. In the present invention, the strongly basic anion exchange resin preferably includes a 201 × 7 ion exchange resin or a D261 ion exchange resin.
In the present invention, the adsorption contact time of the adsorption-elution step is preferably 3 to 10min, and more preferably 3 to 5min; the rinsing contact time is preferably 30 to 45min.
In the present invention, the eluting agent used in the adsorption-elution process is preferably a mixed solution of sulfuric acid and sodium chloride. In the invention, the concentration of the sulfuric acid in the mixed solution of the sulfuric acid and the sodium chloride is preferably 5-10 g/L, and more preferably 5g/L; the concentration of sodium chloride is preferably 50 to 80g/L, more preferably 60g/L. The invention preferably takes 4 bed volumes near the leaching peak uranium concentration as the high uranium concentrated solution.
In the present invention, the temperature of the precipitation is preferably 20 to 35 ℃; the precipitation time is preferably 3 to 6 hours. In the present invention, the pH at the end of the precipitation is preferably 8.
In the invention, the solution in each process is preferably recycled, and the solid waste output is mainly concentrated in the hydrometallurgy tailings.
The technical solution of the present invention will be clearly and completely described below with reference to the embodiments of the present invention. It is to be understood that the described embodiments are merely exemplary of the invention, and not restrictive of the full scope of the invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Example 1
The uranium grade in the iron-boron-containing uranium bulk concentrate is 0.209wt%, and the iron grade is 37.25wt%; according to the process shown in the figure 1, carrying out hot-pressing oxygen leaching on the iron-boron-uranium-containing bulk concentrate, and carrying out solid-liquid separation to obtain uranium-containing leachate and hydrometallurgy tailings; 70wt% of ore with the granularity of-200 meshes and 92wt% of uranium distribution rate (the proportion of uranium of-200 meshes to the total uranium); the leaching process conditions are as follows: the method comprises the following steps of (1) preparing a 2% sulfuric acid solution (the mass of sulfuric acid is 2% of that of the mixed concentrate containing iron, boron and uranium), wherein the reaction temperature is 120 ℃, the oxygen partial pressure is 0.9MPa, the leaching time is 5h, and the liquid-solid ratio is 1;
the leaching rate of uranium is 98.5%, and the iron concentration in the uranium-bearing leaching liquid is 0.12g/L.
Example 2
The uranium grade in the iron-boron-uranium-containing bulk concentrate is 0.225wt%, and the iron grade is 41.05wt%; according to the process shown in fig. 1, carrying out hot-pressing oxygen leaching on the iron-boron-uranium-containing bulk concentrate, and carrying out solid-liquid separation to obtain a uranium-containing leachate and hydrometallurgy tailings; 76wt% of ore with the granularity of-200 meshes and 95wt% of uranium distribution rate (the proportion of uranium with the granularity of-200 meshes to the total uranium); the leaching process conditions are as follows: 1% sulfuric acid solution (the mass of sulfuric acid is 1% of the mass of the mixed concentrate containing iron, boron and uranium), the reaction temperature is 145 ℃, the oxygen partial pressure is 0.5MPa, the leaching time is 3h, and the liquid-solid ratio is 1;
the leaching rate of uranium is 99.2 percent, and the iron concentration in the uranium-bearing leaching liquid is 0.08g/L.
Example 3
The uranium grade in the iron-boron-containing uranium bulk concentrate is 0.209wt%, and the iron grade is 37.25wt%; 70wt% of ore with the granularity of-200 meshes and 92wt% of uranium distribution rate (the proportion of uranium of-200 meshes to the total uranium); according to the process shown in fig. 2, the iron-boron-uranium mixed concentrate is subjected to hot-pressing oxygen leaching, and the leaching process conditions are as follows: the method comprises the following steps of (1) preparing a 2% sulfuric acid solution (the mass of sulfuric acid is 2% of that of the mixed concentrate containing iron, boron and uranium), wherein the reaction temperature is 120 ℃, the oxygen partial pressure is 0.9MPa, the leaching time is 5h, and the liquid-solid ratio is 1; then the leached ore pulp is subjected to solid-liquid separation, and uranium-containing leaching is carried outSubjecting the solution to 201 × 7 ion exchange resin for 5min, eluting with 5g/LH 2 SO 4 And (5) leaching and contacting for 45min with +60g/LNaCl to obtain a high-uranium aggregate solution, and precipitating with sodium hydroxide to obtain a uranium product.
The result shows that the recovery rate of uranium is 95.4%, and the uranium grade of hydrometallurgy tailings is 0.0038%.
Example 4
The uranium grade in the iron-boron-containing uranium bulk concentrate is 0.225wt%, and the iron grade is 41.05wt%; 76wt% of ore with granularity of-200 meshes and 95wt% of uranium distribution rate (the proportion of uranium of-200 meshes to the total uranium); according to the process shown in fig. 2, the iron-boron-uranium mixed concentrate is subjected to hot-pressing oxygen leaching, and the leaching process conditions are as follows: 1% sulfuric acid solution (the mass of sulfuric acid is 1% of the mass of the mixed concentrate containing iron, boron and uranium), the reaction temperature is 145 ℃, the oxygen partial pressure is 0.5MPa, the leaching time is 3h, and the liquid-solid ratio is 1; then carrying out solid-liquid separation on the leached ore pulp, enabling the uranium-containing leachate to pass through D261 ion exchange resin, enabling the contact time to be 3min, and adopting 5g/LH as eluent 2 SO 4 And (5) leaching and contacting for 30min by 60g/LNaCl to obtain high-uranium aggregate liquid, and precipitating by sodium hydroxide to obtain a uranium product.
The result shows that the recovery rate of uranium is 96.1%, and the grade of uranium in the hydrometallurgy tailings is 0.0029%.
The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, various modifications and amendments can be made without departing from the principle of the present invention, and these modifications and amendments should also be considered as the protection scope of the present invention.
Claims (10)
1. The method for efficiently purifying uranium from the iron, boron and uranium containing bulk concentrate is characterized by comprising the following steps of:
carrying out hot-pressing oxygen leaching on the iron-boron-uranium-containing bulk concentrate, and carrying out solid-liquid separation to obtain uranium-containing leachate and hydrometallurgy tailings; the leaching agent adopted by the hot-pressing oxygen leaching is sulfuric acid solution; the hot-pressing oxygen leaching temperature is 120-145 ℃, the leaching time is 1-6 h, and the oxygen partial pressure is 0.2-1.5 MPa.
2. The method according to claim 1, wherein the grade of iron in the iron-boron-uranium containing bulk concentrate is 10-42 wt% and the grade of uranium is 0.1-0.3 wt%.
3. The method of claim 1, wherein the mass of the sulfuric acid is 0.5-6% of the mass of the iron-boron-containing uranium bulk concentrate.
4. The method of claim 1, wherein the hot pressure oxygen leach has a liquid to solid ratio of 1 to 3:1.
5. the method according to any one of claims 1 to 4, wherein after obtaining the uranium containing leach solution, the method further comprises: carrying out ion exchange on the uranium-containing leaching solution to obtain a high-uranium aggregate solution; and precipitating uranium from the high-uranium concentrated solution by using caustic soda flakes or sodium hydroxide particles to obtain a uranium product.
6. The method of claim 5, wherein the ion exchange comprises: and (3) carrying out an adsorption-leaching process on the uranium-containing leaching solution by adopting strong-base anion exchange resin.
7. The method according to claim 6, wherein the adsorption-leaching process has an adsorption contact time of 3 to 10min; the leaching contact time is 30-45 min.
8. The method according to claim 6 or 7, wherein the eluting solution used in the adsorption-elution process is a mixed solution of sulfuric acid and sodium chloride.
9. The method according to claim 8, wherein the concentration of sulfuric acid in the eluent is 5-10 g/L; the concentration of the sodium chloride is 50-80 g/L.
10. The method according to claim 5, wherein the temperature of the precipitation is 20 to 35 ℃; the precipitation time is 3-6 h.
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| CN202211579813.1A CN115874071A (en) | 2022-12-09 | 2022-12-09 | Method for efficiently purifying uranium from iron-boron-uranium-containing bulk concentrate |
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| RU2200204C2 (en) * | 2000-08-07 | 2003-03-10 | Акционерное общество открытого типа "Приаргунское производственное горно-химическое объединение" | Method of processing uranium ores |
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| CN102876890A (en) * | 2012-10-24 | 2013-01-16 | 南华大学 | Method for recovering uranium from beryllium uranium ore with wet process |
| CN106507811B (en) * | 2011-10-27 | 2014-07-23 | 核工业北京化工冶金研究院 | A kind of method of efficient Leaching Uranium in ferro-boron refined ore from uranium-bearing |
| CN106756129A (en) * | 2016-12-28 | 2017-05-31 | 核工业北京化工冶金研究院 | A kind of method that uranium is extracted from stone containing betafite |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| US4321235A (en) * | 1977-02-09 | 1982-03-23 | Compagnie Generale Des Matieres Nucleaires (Cogema) | Process for the treatment of alkaline liquors containing sulfate ions |
| RU2159215C2 (en) * | 1999-02-01 | 2000-11-20 | АООТ "Приаргунское производственное горно-химическое объединение" | Method of hydrometallurgical processing of uranium ores |
| RU2200204C2 (en) * | 2000-08-07 | 2003-03-10 | Акционерное общество открытого типа "Приаргунское производственное горно-химическое объединение" | Method of processing uranium ores |
| WO2011116426A1 (en) * | 2010-03-24 | 2011-09-29 | Bhp Billiton Olympic Dam Corporation Pty Ltd | Process for leaching refractory uraniferous minerals |
| CN106507811B (en) * | 2011-10-27 | 2014-07-23 | 核工业北京化工冶金研究院 | A kind of method of efficient Leaching Uranium in ferro-boron refined ore from uranium-bearing |
| CN102876891A (en) * | 2012-10-24 | 2013-01-16 | 南华大学 | Method for recycling uranium in beryllium and uranium ores by agitation leaching |
| CN102876890A (en) * | 2012-10-24 | 2013-01-16 | 南华大学 | Method for recovering uranium from beryllium uranium ore with wet process |
| CN106756129A (en) * | 2016-12-28 | 2017-05-31 | 核工业北京化工冶金研究院 | A kind of method that uranium is extracted from stone containing betafite |
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