CN108677010A - A kind of ground-dipping uranium extraction comprehensive recycling process - Google Patents
A kind of ground-dipping uranium extraction comprehensive recycling process Download PDFInfo
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- CN108677010A CN108677010A CN201810614661.1A CN201810614661A CN108677010A CN 108677010 A CN108677010 A CN 108677010A CN 201810614661 A CN201810614661 A CN 201810614661A CN 108677010 A CN108677010 A CN 108677010A
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- rhenium
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- recycling process
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- 229910052770 Uranium Inorganic materials 0.000 title claims abstract description 50
- JFALSRSLKYAFGM-UHFFFAOYSA-N uranium(0) Chemical compound [U] JFALSRSLKYAFGM-UHFFFAOYSA-N 0.000 title claims abstract description 50
- 238000000605 extraction Methods 0.000 title claims abstract description 37
- 238000000034 method Methods 0.000 title claims abstract description 23
- 238000007598 dipping method Methods 0.000 title claims abstract description 22
- 238000004064 recycling Methods 0.000 title claims abstract description 21
- 229910052702 rhenium Inorganic materials 0.000 claims abstract description 112
- WUAPFZMCVAUBPE-UHFFFAOYSA-N rhenium atom Chemical compound [Re] WUAPFZMCVAUBPE-UHFFFAOYSA-N 0.000 claims abstract description 112
- 239000007788 liquid Substances 0.000 claims abstract description 36
- 238000001179 sorption measurement Methods 0.000 claims abstract description 34
- 239000012074 organic phase Substances 0.000 claims abstract description 22
- 239000011347 resin Substances 0.000 claims abstract description 20
- 229920005989 resin Polymers 0.000 claims abstract description 20
- 239000011259 mixed solution Substances 0.000 claims abstract description 18
- WPWNMJMTCOIAEI-UHFFFAOYSA-N [Re].[U] Chemical compound [Re].[U] WPWNMJMTCOIAEI-UHFFFAOYSA-N 0.000 claims abstract description 16
- 229920006395 saturated elastomer Polymers 0.000 claims abstract description 14
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 claims abstract description 11
- 239000002253 acid Substances 0.000 claims abstract description 11
- 229910052700 potassium Inorganic materials 0.000 claims abstract description 11
- 239000011591 potassium Substances 0.000 claims abstract description 11
- 239000012071 phase Substances 0.000 claims abstract description 8
- 239000000284 extract Substances 0.000 claims abstract description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 7
- 238000002386 leaching Methods 0.000 claims abstract description 4
- KFZMGEQAYNKOFK-UHFFFAOYSA-N Isopropanol Chemical compound CC(C)O KFZMGEQAYNKOFK-UHFFFAOYSA-N 0.000 claims description 16
- 239000003480 eluent Substances 0.000 claims description 13
- WCUXLLCKKVVCTQ-UHFFFAOYSA-M Potassium chloride Chemical compound [Cl-].[K+] WCUXLLCKKVVCTQ-UHFFFAOYSA-M 0.000 claims description 10
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 8
- 238000010521 absorption reaction Methods 0.000 claims description 8
- 239000003957 anion exchange resin Substances 0.000 claims description 8
- 239000003153 chemical reaction reagent Substances 0.000 claims description 7
- VWDWKYIASSYTQR-UHFFFAOYSA-N sodium nitrate Inorganic materials [Na+].[O-][N+]([O-])=O VWDWKYIASSYTQR-UHFFFAOYSA-N 0.000 claims description 7
- 230000002195 synergetic effect Effects 0.000 claims description 7
- 150000001875 compounds Chemical class 0.000 claims description 6
- 239000003085 diluting agent Substances 0.000 claims description 5
- 238000010828 elution Methods 0.000 claims description 5
- 239000003350 kerosene Substances 0.000 claims description 5
- 239000001103 potassium chloride Substances 0.000 claims description 5
- 235000011164 potassium chloride Nutrition 0.000 claims description 5
- 239000000243 solution Substances 0.000 claims description 5
- 229910021529 ammonia Inorganic materials 0.000 claims description 4
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 3
- 239000000908 ammonium hydroxide Substances 0.000 claims description 3
- 239000003795 chemical substances by application Substances 0.000 claims description 2
- 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 claims 1
- PEDCQBHIVMGVHV-UHFFFAOYSA-N Glycerine Chemical compound OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 claims 1
- 239000003456 ion exchange resin Substances 0.000 claims 1
- 229920003303 ion-exchange polymer Polymers 0.000 claims 1
- 238000011065 in-situ storage Methods 0.000 abstract description 2
- 238000000926 separation method Methods 0.000 abstract description 2
- 229910052751 metal Inorganic materials 0.000 description 4
- 239000002184 metal Substances 0.000 description 4
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 description 2
- 239000003463 adsorbent Substances 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 229910052750 molybdenum Inorganic materials 0.000 description 2
- 239000011733 molybdenum Substances 0.000 description 2
- 238000001556 precipitation Methods 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 1
- BUGBHKTXTAQXES-UHFFFAOYSA-N Selenium Chemical compound [Se] BUGBHKTXTAQXES-UHFFFAOYSA-N 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 1
- 230000033558 biomineral tissue development Effects 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 239000010949 copper Substances 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 235000010755 mineral Nutrition 0.000 description 1
- KTEXACXVPZFITO-UHFFFAOYSA-N molybdenum uranium Chemical compound [Mo].[U] KTEXACXVPZFITO-UHFFFAOYSA-N 0.000 description 1
- 239000012452 mother liquor Substances 0.000 description 1
- 238000009853 pyrometallurgy Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 229910052706 scandium Inorganic materials 0.000 description 1
- SIXSYDAISGFNSX-UHFFFAOYSA-N scandium atom Chemical compound [Sc] SIXSYDAISGFNSX-UHFFFAOYSA-N 0.000 description 1
- 229910052711 selenium Inorganic materials 0.000 description 1
- 239000011669 selenium Substances 0.000 description 1
- 235000010344 sodium nitrate Nutrition 0.000 description 1
- 235000011149 sulphuric acid Nutrition 0.000 description 1
- 230000007704 transition Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 229910052727 yttrium Inorganic materials 0.000 description 1
- VWQVUPCCIRVNHF-UHFFFAOYSA-N yttrium atom Chemical compound [Y] VWQVUPCCIRVNHF-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- 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
- C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
- C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
- C22B3/42—Treatment or purification of solutions, e.g. obtained by leaching by ion-exchange extraction
-
- 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
- C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
- C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
- C22B3/26—Treatment or purification of solutions, e.g. obtained by leaching by liquid-liquid extraction using organic compounds
- C22B3/28—Amines
-
- 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
- C22B60/00—Obtaining metals of atomic number 87 or higher, i.e. radioactive metals
- C22B60/02—Obtaining thorium, uranium, or other actinides
-
- 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
- C22B61/00—Obtaining metals not elsewhere provided for in this subclass
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Mechanical Engineering (AREA)
- Manufacturing & Machinery (AREA)
- Materials Engineering (AREA)
- Metallurgy (AREA)
- Organic Chemistry (AREA)
- Geology (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Life Sciences & Earth Sciences (AREA)
- Geochemistry & Mineralogy (AREA)
- Manufacture And Refinement Of Metals (AREA)
Abstract
The present invention relates to in-situ leaching uranium technical fields, specifically disclose a kind of ground-dipping uranium extraction comprehensive recycling process, include the following steps：(1) resin adsorption rhenium；(2) saturated resin elutes；(3) uranium rhenium mixed solution extracts；(4) rhenium-containing organic phase is stripped；(5) rehenic acid potassium is obtained.The method of the present invention realizes the enrichment of rhenium, and rhenium concentration reaches 1000 times of rhenium concentration in rhenium-containing adsorption tail liquid or more in rhenium-containing product liquid, and the separation of rhenium and uranium is realized by extraction process, and 99% or more uranium stays in raffinate water phase, does not enter organic phase.
Description
Technical field
The invention belongs to in-situ leaching uranium technical fields, and in particular to a kind of ground-dipping uranium extraction comprehensive recycling process, from containing
Rhenium metal is recycled in uranium absorption tail washings.
Background technology
Rhenium metal is widely used in the fields such as national defence, space flight and aviation, high-energy physics and nuclear industry due to its unique property.
In nature, the mineral resources of rhenium lack, and abundance is only 7 × 10 in the earth's crust-8, and most of rhenium is deposited in the form of impurity is disseminated
.Currently, the raw material type of extraction rhenium is rare, the flue gas washing liquid predominantly in copper pyrometallurgy and rhenium-containing molybdenum ore.With work
The development of industry, the increasingly increase to rhenium demand, the market price reach ten thousand yuan/ton of 6000-7000.
Years of researches practice have shown that, sandrock-type uranium deposit is in addition to uranium, there are many more accompanying element, as scandium, selenium, rhenium,
Yttrium, molybdenum etc..The distribution of rhenium, general presentation and the completely equitant web-like of uranium ore layer or stratiform, occupy the transition position between uranium molybdenum
It sets.In the section of ledge, rhenium mineralising thickness is usually bigger than the thickness of uranium mineralization.
Uvanas, Mynkuduk and Moyinkum uranium deposit of Kazakhstan find that accompanying element rhenium, grade reach
0.1-0.5g/t ores.The Zajistan uranium deposit and Wukurqi uranium deposit in China, it has been found that accompanying element rhenium.Recycle sandstone
The rhenium of type uranium deposit association finds a new way for extension rhenium resource.
During ground-dipping uranium extraction, while uranium is leached, the rhenium in ore is also leached, with ReO4-Form enters leachate
In.Rhenium is primarily present in the poor resin after adsorption tail liquid, scrubbed uranium and the mother liquor of precipitation of ammonium after precipitation uranium.Wherein,
90% or more rhenium is present in the later adsorption tail liquid of adsorption uranium.Current production technology is difficult to realize to the effective of rhenium metal
Recycling is a kind of greatly waste to resource.
Invention content
The purpose of the present invention is to provide a kind of ground-dipping uranium extraction comprehensive recycling process, can be from ground-dipping uranium extraction adsorption tail liquid
Recycle associated metal element rhenium.
Technical scheme is as follows：
A kind of ground-dipping uranium extraction comprehensive recycling process, includes the following steps：
(1) resin adsorption rhenium
The ground leaching adsorption tail liquid of rhenium-containing is by adsorption tower, using anion exchange resin Adsorption of Rhenium, until adsorption tower goes out liquid
When the concentration difference of rhenium in the concentration and feed liquor of middle rhenium≤2%, stops absorption, obtain rhenium-containing saturated resin；
(2) saturated resin elutes
Use NaNO3And H2SO4Solution elutes rhenium-containing saturated resin, obtains uranium rhenium mixed solution as eluent；
(3) uranium rhenium mixed solution extracts
Using di-tertiary amine class compound as extractant, isopropanol is as synergic reagent, and kerosene is as diluent, extraction step
(2) rhenium in the mixed solution of uranium rhenium described in, obtains rhenium-containing organic phase；
(4) rhenium-containing organic phase is stripped
Using ammonium hydroxide as strippant, the rhenium being stripped in organic phase obtains rhenium-containing product liquid；
(5) rehenic acid potassium is obtained
Potassium chloride is added in the rhenium-containing product liquid obtained into step (4), obtains rehenic acid potassium product.
Anion exchange resin described in step (1) is macroporous anion exchange resin D355.
Adsorption tail liquid flow control is in 3~10BV/h in step (1).
NaNO in step (2) eluent3A concentration of 40~80g/L, H2SO4A concentration of 50~100g/L.
For the flow control of eluent in 0.1~0.5BV/h, elution volume is 3~5 BV, eluent temperature in step (2)
It is 40~60 DEG C.
8~15%, the volume fraction of synergic reagent is controlled 5 for the volume fraction control of extractant described in step (3)
~10%, stream is controlled than O/W 1/5~1/40.
99% or more uranium stays in raffinate water phase in step (3), does not enter organic phase.
Strippant ammonia concn described in step (4) is 1~2mol/L, and stream is controlled than O/W 3/1~5/1.
Extraction described in step (3) is extracted using multistage counter current.
Rhenium concentration soaks 1000 of rhenium concentration in adsorption tail liquid with reaching rhenium-containing in the rhenium-containing product liquid obtained by step (4)
Times or more.
The remarkable result of the present invention is：
(1) the method for the present invention realizes the enrichment of rhenium, and it is dense to reach rhenium in rhenium-containing adsorption tail liquid for rhenium concentration in rhenium-containing product liquid
1000 times or more of degree；
(2) the method for the present invention realizes the separation of rhenium and uranium by extraction process, and 99% or more uranium stays in raffinate water phase
In, do not enter organic phase.
Description of the drawings
Fig. 1 is a kind of flow diagram of ground-dipping uranium extraction comprehensive recycling process of the present invention.
Specific implementation mode
Below in conjunction with the accompanying drawings and specific embodiment invention is further described in detail.
A kind of ground-dipping uranium extraction comprehensive recycling process as shown in Figure 1, includes the following steps：
1. resin adsorption rhenium
The ground of rhenium-containing soaks adsorption tail liquid by adsorption tower, uses anion exchange resin Adsorption of Rhenium；Flow control 3~
10BV/h stops absorption, it is full to obtain rhenium-containing until when adsorption tower goes out the concentration difference of rhenium in the concentration of rhenium and feed liquor in liquid≤2%
And resin.
2. saturated resin elutes
Use NaNO3And H2SO4Solution elutes rhenium-containing saturated resin, flow control is in 0.1~0.5BV/ as eluent
H, elution volume are 3~5 BV, obtain uranium rhenium mixed solution.In eluent, a concentration of 40~80g/L of NaNO3, H2SO4 concentration
For 50~100g/L, eluent temperature is 40~60 DEG C.
3. uranium rhenium mixed solution extracts
Using di-tertiary amine class compound as extractant, isopropanol is obtained by extraction as synergic reagent, kerosene as diluent
Rhenium in the mixed solution of uranium rhenium described in step 2；The volume fraction control of extractant di-tertiary amine class compound is assisted 8~15%
Extract the volume fraction control of agent isopropanol 5~10%, stream is controlled than O/W 1/5~1/40, obtains rhenium-containing organic phase；99%
Above uranium stays in raffinate water phase, does not enter organic phase.
4. rhenium-containing organic phase is stripped
Using 1~2mol/L ammonium hydroxide as strippant, stream, 3/1~5/1, is stripped in organic phase than O/W controls
Rhenium obtains rhenium-containing product liquid.
5. obtaining rehenic acid potassium
Potassium chloride is added into the rhenium-containing product liquid obtained in step 4, obtains rehenic acid potassium product.
Embodiment 1
One kind is comprised the following steps that from ground-dipping uranium extraction comprehensive recycling process：
1, the absorption of rhenium
Rhenium-containing adsorption tail liquid is by adsorption tower, and flow control is in 5BV/h；A concentration of 0.74mg/L of rhenium, uranium in adsorption tail liquid
A concentration of 0.92mg/L, pH value 2.10；Using the rhenium in macroporous anion exchange resin D355 adsorbent solutions, until adsorption tower
When going out the concentration difference of rhenium in liquid and feed liquor≤2%, stops absorption, obtain rhenium-containing saturated resin.
2, rhenium-containing saturated resin elutes
Use 40 DEG C of 42g/LNaNO3And 60g/LH2SO4Mixed solution elutes rhenium-containing saturated resin as eluent；Stream
Speed control obtains uranium rhenium mixed solution, elution volume 4.2BV in 0.4BV/h；Wherein uranium concentration is 130.5mg/L, rhenium concentration
For 29.2mg/L.
3, uranium rhenium mixed solution extracts
Using di-tertiary amine class compound as extractant, isopropanol is synergic reagent, and kerosene is as diluent；Di-tertiary amine class
It is 12% to close object fraction, and isopropanol volume fraction is 6%；Extraction uses 4 sections of counter-current extractions, and stream is than O/W=1/20, extraction
(2) rhenium in uranium rhenium mixed solution in, obtains rhenium-containing organic phase；99% or more uranium stays in raffinate water phase, has not entered
Machine phase.
4, rhenium-containing organic phase is stripped
Using the ammonia spirit of 1.2mol/L as strippant, stream is stripped than O/W=3/1 in rhenium-containing organic phase
Rhenium obtains rhenium-containing product liquid, a concentration of 2.27g/L of rhenium；
5, rehenic acid potassium is obtained
Potassium chloride is added into the rhenium-containing product liquid obtained in step 4, obtains rehenic acid potassium product.
Embodiment 2
One kind is comprised the following steps that from ground-dipping uranium extraction comprehensive recycling process：
1, the absorption of rhenium
Rhenium-containing adsorption tail liquid is by adsorption tower, and flow control is in 6BV/h；A concentration of 0.54mg/L of rhenium, uranium in adsorption tail liquid
A concentration of 0.56mg/L, pH value 1.95；Using the rhenium in anion exchange resin D355 adsorbent solutions, until adsorption tower goes out liquid
With the concentration of rhenium in feed liquor it is poor≤2% when, stop absorption.
2, rhenium-containing saturated resin elutes
Use 50 DEG C of 50g/L NaNO3With 80g/L H2SO4Mixed solution elutes saturated resin as eluent；Flow velocity
Control obtains uranium rhenium mixed solution, elution volume 3.8BV in 0.3BV/h；Uranium concentration is 98.6mg/L, and rhenium is a concentration of
23.2mg/L。
3, uranium rhenium mixed solution extracts
Using di-tertiary amine class compound as extractant, isopropanol is synergic reagent, and kerosene is as diluent；Di-tertiary amine class
It is 15% to close object fraction, and isopropanol volume fraction is 8%；Extraction uses 3 sections of counter-current extractions, and stream is than O/W=1/30, extraction
The rhenium in uranium rhenium mixed solution in step 2, obtains rhenium-containing organic phase；99% or more uranium stays in raffinate water phase, does not enter
Organic phase.
4, rhenium-containing organic phase is stripped
Using the ammonia spirit of 1.5mol/L as strippant, stream is stripped than O/W=3/1 in rhenium-containing organic phase
Rhenium obtains rhenium-containing product liquid, a concentration of 1.61g/L of rhenium.
5, rehenic acid potassium is obtained
Potassium chloride is added into the rhenium-containing product liquid obtained in step 4, obtains rehenic acid potassium product.
Claims (10)
1. a kind of ground-dipping uranium extraction comprehensive recycling process, it is characterised in that：Include the following steps：
(1) resin adsorption rhenium
The ground leaching adsorption tail liquid of rhenium-containing is by adsorption tower, using anion exchange resin Adsorption of Rhenium, until adsorption tower goes out rhenium in liquid
Concentration and feed liquor in rhenium concentration difference≤2% when, stop absorption, obtain rhenium-containing saturated resin；
(2) saturated resin elutes
Use NaNO3And H2SO4Solution elutes rhenium-containing saturated resin, obtains uranium rhenium mixed solution as eluent；
(3) uranium rhenium mixed solution extracts
Using di-tertiary amine class compound as extractant, isopropanol is as synergic reagent, and kerosene is as diluent, extraction step (2)
Described in rhenium in uranium rhenium mixed solution, obtain rhenium-containing organic phase；
(4) rhenium-containing organic phase is stripped
Using ammonium hydroxide as strippant, the rhenium being stripped in organic phase obtains rhenium-containing product liquid；
(5) rehenic acid potassium is obtained
Potassium chloride is added in the rhenium-containing product liquid obtained into step (4), obtains rehenic acid potassium product.
2. a kind of ground-dipping uranium extraction comprehensive recycling process as described in claim 1, it is characterised in that：The moon described in step (1)
Ion exchange resin is macroporous anion exchange resin D355.
3. a kind of ground-dipping uranium extraction comprehensive recycling process as claimed in claim 2, it is characterised in that：Adsorption tail liquid in step (1)
Flow control is in 3~10BV/h.
4. a kind of ground-dipping uranium extraction comprehensive recycling process as claimed in claim 3, it is characterised in that：In step (2) eluent
NaNO3A concentration of 40~80g/L, H2SO4A concentration of 50~100g/L.
5. a kind of ground-dipping uranium extraction comprehensive recycling process as claimed in claim 4, it is characterised in that：Eluent in step (2)
For flow control in 0.1~0.5BV/h, elution volume is 3~5 BV, and eluent temperature is 40~60 DEG C.
6. a kind of ground-dipping uranium extraction comprehensive recycling process as claimed in claim 5, it is characterised in that：Extraction described in step (3)
Take the volume fraction of agent to control 8~15%, the volume fraction control of synergic reagent 5~10%, stream than O/W controls 1/5~
1/40。
7. a kind of ground-dipping uranium extraction comprehensive recycling process as claimed in claim 6, it is characterised in that：99% or more in step (3)
Uranium stay in raffinate water phase, do not enter organic phase.
8. a kind of ground-dipping uranium extraction comprehensive recycling process as claimed in claim 7, it is characterised in that：It is anti-described in step (4)
Extractant ammonia concn is 1~2mol/L, and stream is controlled than O/W 3/1~5/1.
9. a kind of ground-dipping uranium extraction comprehensive recycling process as claimed in claim 8, it is characterised in that：Extraction described in step (3)
It takes and is extracted using multistage counter current.
10. a kind of ground-dipping uranium extraction comprehensive recycling process as claimed in claim 9, it is characterised in that：It is obtained by step (4)
Rhenium concentration soaks 1000 times of rhenium concentration in adsorption tail liquid or more with reaching rhenium-containing in rhenium-containing product liquid.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113584330A (en) * | 2020-11-30 | 2021-11-02 | 核工业北京化工冶金研究院 | From CO2+O2Method for comprehensively recovering rhenium from in-situ leaching uranium mining leachate |
| CN114686681A (en) * | 2020-12-30 | 2022-07-01 | 中核通辽铀业有限责任公司 | Remote uranium deposit resource recovery system and method |
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| CN101050489A (en) * | 2007-05-18 | 2007-10-10 | 锦州沈宏集团股份有限公司 | Method for extracting rhenium from eluate of flue ash generated by baking enriched ore of molybdenum |
| CN102433439A (en) * | 2011-12-16 | 2012-05-02 | 湖南有色金属研究院 | Method for recovering rhenium from arsenic filter cake |
| CN105671324A (en) * | 2016-03-07 | 2016-06-15 | 紫金矿业集团股份有限公司 | Method for preparing ammonium rhenate from rhenium-enriched slags |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN113584330A (en) * | 2020-11-30 | 2021-11-02 | 核工业北京化工冶金研究院 | From CO2+O2Method for comprehensively recovering rhenium from in-situ leaching uranium mining leachate |
| CN114686681A (en) * | 2020-12-30 | 2022-07-01 | 中核通辽铀业有限责任公司 | Remote uranium deposit resource recovery system and method |
| CN114686681B (en) * | 2020-12-30 | 2023-10-20 | 中核通辽铀业有限责任公司 | Remote uranium deposit resource recovery system and method |
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