CN103846081B - A kind of D382 type resin acidic resolves technique - Google Patents
A kind of D382 type resin acidic resolves technique Download PDFInfo
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- CN103846081B CN103846081B CN201210518105.7A CN201210518105A CN103846081B CN 103846081 B CN103846081 B CN 103846081B CN 201210518105 A CN201210518105 A CN 201210518105A CN 103846081 B CN103846081 B CN 103846081B
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Abstract
The invention provides a kind of D382 type resin easy and simple to handle and the parsing of environmental protection, transformation process when " high mineralization, high chlorine root " alkaline Leaching.The progressive part of the present invention is in that to simplify parsing technique, reduces resolution flow ratio, improves qualifying liquid uranium concentration, eliminates the consumption of technique salt and ammonium hydrogen carbonate；Resolving compared with technique with alkalescence, reduce production cost, alleviate the working strength of employee, eliminate the discharge of ammonia, operating process is simpler and environmental protection.
Description
Technical field
The invention belongs to ground-dipping uranium extraction hydrometallurgy processing technology field, be specifically related to the parsing when " high mineralization, high chlorine root " alkaline Leaching of the D382 type resin, transformation process.
Background technology
Acid in-situ leaching technology obtains successfully at Yi Li uranium mine and develops rapidly in the whole nation, but certain mine increasingly complex at geological conditions can only by weak reagent meutral innersion technique, this mine grade of ore is low simultaneously, leachate uranium concentration is low, " the high salinity of leachate, high chloride ion " make major part resin not adsorption uranium substantially, D382 type resin is have developed under Hua Ye institute cooperates, this model resin leachate aftertreatment technology flow process is taked to can adapt in this mineral deposit " high salinity, high chloride ion " content leachate process, and disclosure satisfy that in " low concentration, big flow " leachate process conditions.But industrial experiment initial stage resin treatment need to be undertaken in two steps, sodium chloride adds carbonic acid oronain and carries out alkalescence parsing, then makes the transition with technical hydrochloric acid again, this technological process is too much, troublesome poeration, and workload is big, raw-material consumption is big, and the unfavorable workman of operating process ammonia emission is physically and mentally healthy.Therefore, a kind of toxic emission minimizing need to be developed in pole, operation easily operates and the D382 type resin acidic of more environmental protection resolves technique.
Summary of the invention
It is an object of the invention to overcome the defect of prior art, it is provided that a kind of D382 type resin easy and simple to handle and the parsing of environmental protection, transformation process when " high mineralization, high chlorine root " alkaline Leaching.
To achieve these goals, the technical scheme is that, a kind of D382 type resin acidic resolves technique, comprises the steps of
Step 1, after D382 type resin absorption is saturated, clears up impurity such as the silts being adsorbed in resin particle gap through backwash operation, afterwards with the compression air of 0.2MPa pressure by standby for the drain in resin particle gap；
Step 2, becomes acidifying solution by qualifying liquid, technical hydrochloric acid according to the proportions of volume ratio 14～16:3, after the adsorption tower comprising D382 type resin must satisfied be completely filled with by the volume of configuration acidifying solution, also has 1m3Surplus；Then delivering in adsorption tower by the acidifying solution of wherein 60%, the D382 type resin after step 1 processes is soaked, soak time is 6～8 hours；
Step 3, by adsorption tower and outside adsorption tower acidifying solution be circulated, endless form adopts lower feed liquor, above goes out the mode of liquid；Circulation fluid pH is monitored, when feed liquor stops circulation with going out when liquid pH value reaches consistent and≤1.5 after circulating 6～8 hours；If pH value is below standard, add 0.5m3Technical hydrochloric acid, continues cycling through, until feed liquor with go out liquid pH value reach consistent and≤1.5 time；
Step 4, completes to enter after step 3 to resolve operation, resolves operation and selects that to resolve agent be the hydrochloric acid solution of 3～4g/L, adopts three tower cascade connected parsing, analysis mode adopt upper feed liquor, under go out liquid, in adsorption tower, the linear velocity of desorbed solution is 0.8～1.0m/h；Stop when parsing liquid flowing ratio and reaching about 2 into parsing agent, it is thus achieved that resolve qualifying liquid；Then entering the compression air of 0.2MP to the first tower in three towers, continue to resolve, go out liquid to acidifying solution storage tank, processing industry hydrochloric acid is configured to the parsing after acidifying solution for other adsorption towers；Entrance pressure contracting air terminates to resolve operation after being pressed dry by head tower, proceeds to step 5；
Step 5, to first tower injected clear water washing, linear velocity is 2m/h, can stop more than 4.0 until going out liquid uranium concentration less than 1mg/L and pH value；
Step 6, parsing qualifying liquid step 4 obtained carries out neutral precipitation: add the stirring of NaOH limit, pH value determination after stirring toward resolving limit in qualifying liquid, until when pH value is 7.0～8.0, stopping adding NaOH and stirring, precipitating；After precipitating 12 hours, discharge supernatant, then add the parsing qualifying liquid of same volume, repeat the neutral settling step in this step, after reaching 70 times until precipitation number of times, carry out filter press operation and obtain product.
In described step 3, when feed liquor stops circulation with going out when liquid pH value reaches consistent and≤1.3.
In described step 4, resolve operation and select parsing agent to be the hydrochloric acid solution of 3.5g/L.
In described step 6, after qualifying liquid precipitation is complete, adds 1.5 times of slurry volume clear water and carry out clear water precipitation, after drained supernatant, then enter filter press operation acquisition product.
The progressive part of the present invention is in that to simplify parsing technique, reduces resolution flow ratio, improves qualifying liquid uranium concentration, eliminates the consumption of technique salt and ammonium hydrogen carbonate；Resolving compared with technique with alkalescence, reduce production cost, alleviate the working strength of employee, eliminate the discharge of ammonia, operating process is simpler and environmental protection.
Detailed description of the invention
Below in conjunction with embodiment, the present invention is described further.
Implement device
A kind of D382 type resin acidic resolves technique, implements by means of following existing device:
A. adsorption tower: adsorption tower is diameter 2.5m iron flask, and height overall is 7.5m, and effective depth is 6m, liner PO, and parts include: interface at the bottom of tower, DN200 flange, for liquid liquid outlet；Tower top interface, DN25, installs Pressure gauge and uses；Tower top interface, DN500 flange, for stock solution inlet；Tower top interface, DN40, it is connected with compressed air piping；Compressed air piping is DN50 iron pipe, and all the other connect pipeline and are PPR pipe, and size is corresponding with flange size.
B. agent storage tank is resolved: diameter 2.5m iron flask, is highly 2m, liner PO, parts bag: tower top interface, and DN40 flange is connected with fresh water pipeline by DN40 iron pipe；Tower top air vent, 40cm*40cm；Interface at the bottom of tower, DN40 flange, resolve agent liquid outlet, the PPR pipe of DN40 be connected with resolving agent delivery pump.
C. acidifying solution storage tank: diameter 2.5m iron flask, high 4m, liner PO, parts include: tower top interface, and DN40 flange is connected with fresh water pipeline by DN40 iron pipe；Tower top interface, DN40 flange, DN40PPR pipeline connect hydrochloric acid pipeline；Tower top air vent, DN50；Tower top interface, DN80 flange, salification cycles backwater, DN80PPR pipeline connect；Interface at the bottom of tower, DN80 flange, acidifying solution goes out liquid use, connects DN80PPR pipeline.
D. stock solution pond: stock solution pond is long 25m, wide 20m, high 3.5m cement tub, parts include: stock solution inlet, long 40cm, wide 40cm；Air vent, long 40cm, wide 40cm；Air vent, long 40cm, wide 40cm；Stock solution liquid outlet, DN200 flange, is docked with entering tower pump by DN200 iron pipe.
E. mother solution pond: the long 6m in mother solution pond, wide 6m, high 2m metal trough, parts include: DN40 iron pipe, clap clear liquid in mother solution pond and use.
F. stillpot: diameter 1.5m, high 3.3m iron flask, liner PO, parts include: tank deck interface, and DN40 flange is connected with qualifying liquid pipeline by DN40PPR pipeline；Tank deck interface, DN40 flange, DN40PPR pipeline it is connected with fresh water pipeline；Tank deck interface, DN40 flange, DN40PPR pipeline it is connected with plate water return pipeline；Tank deck mouth, long 40cm, wide 40cm, precipitation adds sheet alkali and uses；Tank bottoms interface, DN40 flange, re-pack frame grout outlet, DN40PPR pipeline connect.
Implement step
Step 1, after D382 type resin absorption is saturated, clears up impurity such as the silts being adsorbed in resin particle gap through backwash operation, afterwards with the compression air of 0.2MPa pressure by standby for the drain in resin particle gap；
Step 2, certain uranium mine adopts 15m3Uranium concentration is less than adding 3m in the qualifying liquid of 5g/L3The proportions of technical hydrochloric acid becomes the acidifying solution that adsorption tower volume is consistent, by acidifying solution delivery pump by 60% acidifying solution be delivered in adsorption tower resin soaked；Qualifying liquid refer to saturated resin uranium-bearing liquid after resolving agent and resolving in leaching technology, technical hydrochloric acid is mass percent is 31% HCl solution having, soak time 8 hours；；
Step 3, is circulated the acidifying solution in adsorption tower and outside adsorption tower, and endless form adopts lower feed liquor, above goes out the mode of liquid；After circulating 6～8 hours monitor circulation fluid pH, when feed liquor with go out liquid pH value reach consistent and≤preferably 1.3 time stop circulate；If pH value is below standard, add 0.5m3Technical hydrochloric acid, continues cycling through, until feed liquor with go out liquid pH value reach consistent and≤1.3 time；
Step 4, completes to enter after step 3 to resolve operation, resolves operation and selects that to resolve agent be the hydrochloric acid solution of 3.5g/L, adopts three tower cascade connected parsing, analysis mode adopt upper feed liquor, under go out liquid, in adsorption tower, the linear velocity of desorbed solution is 0.8～1.0m/h；When parsing of recording of electronic flowmeter stops into parsing agent when liquid flowing ratio reaches about 2, it is thus achieved that resolve qualifying liquid；Being then turned on air compressor machine, the first tower in Xiang Santa enters the compression air of 0.2MP, continues to resolve, go out liquid to acidifying solution storage tank, processing industry hydrochloric acid is configured to the parsing after acidifying solution for other adsorption towers, and entrance pressure contracting air terminates to resolve operation after being pressed dry by head tower, proceeds to the rinsing process of step 5；In the present embodiment, when first tower press dry, head tower desorbed solution uranium concentration is less than 800mg/L, and the D382 type resin before parsing is saturated resin, becomes lean resin after step 4 resolves, and the first lean resin residue uranium capacity of tower is less than 1g/L；
Step 5, to first tower injected clear water washing, control flow is 10m3/ h, can stop more than 4.0 until going out liquid uranium concentration less than 1mg/L and pH value, to reach to reclaim remaining uranium and the purpose of system pH in raising adsorption tower on resin；
Step 6, parsing qualifying liquid step 4 obtained carries out neutral precipitation: squeeze in stillpot by parsing qualifying liquid pump, add sheet alkali while stirring, qualifying liquid stops feed liquor from stillpot top about 10cm, regulate pH value after stirring 5 minutes to 7.0～8.0, if pH is inadequate, adds appropriate sheet alkali and continue stirring, until pH is up to standard, stops stirring and precipitate；Within 12 hours, heel row supernatant goes to mother solution pond, then adds the step that qualifying liquid continues to repeat above again.Filter press operation can be carried out when precipitating number of times and reaching more than 70 times, reduce product impurity content, improve product grade, after qualifying liquid precipitation is complete, in stillpot, add about 1.5 times of slurry volume clear water carry out clear water precipitation, the frame operation acquisition product that re-packs after drained supernatant, can be carried out.
Result of implementation: the present invention contrasts in Table 1 and table 2 with the alkaline parameter comparison resolving qualifying liquid precipitation products obtained therefrom and economic indicator:
1: two kind of product parameters contrast of table
2 two kinds of process economics indexs of table
As it can be seen from table 1 have some superiority resolve qualifying liquid precipitation products obtained therefrom with alkalescence compared with, product uranium grade can improve about 7%, chloride ion content reduces about 1%.
As can be seen from Table 2, by this technique, alkalescence parsing-acid two-step process that makes the transition is reduced to a step and completes, resolution flow is down to about 2.0 than by about 3, qualifying liquid uranium concentration is brought up to about 12g/L by about 8g/L, eliminate the consumption of technique salt and ammonium hydrogen carbonate, produce uranium per ton compared with resolving technique with alkalescence and can reduce production cost about 1.4 ten thousand yuan, alleviate the working strength of employee simultaneously, eliminating the discharge of ammonia, operating process is simpler and environmental protection.
Above embodiments of the invention are explained in detail, above-mentioned embodiment is only most highly preferred embodiment of the invention, but the present invention is not limited to above-described embodiment, in the ken that those of ordinary skill in the art possess, it is also possible to make various change under the premise without departing from present inventive concept.
Claims (4)
1. a D382 type resin acidic resolves technique, it is characterised in that comprise the steps of
Step 1, after D382 type resin absorption is saturated, through the silt impurity cleaning that backwash operation will be adsorbed in resin particle gap, afterwards with the compression air of 0.2MPa pressure by standby for the drain in resin particle gap；
Step 2, becomes acidifying solution by qualifying liquid, technical hydrochloric acid according to the proportions of volume ratio 14～16:3, after the adsorption tower comprising D382 type resin must satisfied be completely filled with by the volume of preparation acidifying solution, also has 1m3Surplus；Then delivering in adsorption tower by the acidifying solution of wherein 60%, the D382 type resin after step 1 processes is soaked, soak time is 6～8 hours；Qualifying liquid refer to saturated resin uranium-bearing liquid after resolving agent and resolving in leaching technology；Technical hydrochloric acid is mass percent is the HCl solution of 31%；
Step 3, by adsorption tower and outside adsorption tower acidifying solution be circulated, endless form adopts lower feed liquor, above goes out the mode of liquid；Circulation fluid pH value is monitored, when feed liquor stops circulation with going out when liquid pH value reaches consistent and≤1.5 after circulating 6～8 hours；If pH value is below standard, add 0.5m3Technical hydrochloric acid, continues cycling through, until feed liquor with go out liquid pH value reach consistent and≤1.5 time；
Step 4, completes to enter after step 3 to resolve operation, resolves operation and selects that to resolve agent be the hydrochloric acid solution of 3～4g/L, adopts three tower cascade connected parsing, analysis mode adopt upper feed liquor, under go out liquid, in adsorption tower, the linear velocity of desorbed solution is 0.8～1.0m/h；Stop when parsing liquid flowing ratio and reaching 2 into parsing agent, it is thus achieved that resolve qualifying liquid；Then entering the compression air of 0.2MPa to the first tower in three towers, continue to resolve, go out liquid to acidifying solution storage tank, processing industry hydrochloric acid is configured to the parsing after acidifying solution for other adsorption towers；Entrance pressure contracting air terminates to resolve operation after being pressed dry by head tower, proceeds to step 5；
Step 5, to first tower injected clear water washing, linear velocity is 2m/h, can stop more than 4.0 until going out liquid uranium concentration less than 1mg/L and pH value；
Step 6, parsing qualifying liquid step 4 obtained carries out neutral precipitation: add the stirring of NaOH limit, pH value determination after stirring toward resolving limit in qualifying liquid, until when pH value is 7.0～8.0, stopping adding NaOH and stirring, precipitating；After precipitating 12 hours, discharge supernatant, then add the parsing qualifying liquid of same volume, repeat the neutral settling step in this step, after reaching 70 times until precipitation number of times, carry out filter press operation and obtain product.
2. a kind of D382 type resin acidic as claimed in claim 1 resolves technique, it is characterised in that in step 3, when feed liquor stops circulation with going out when liquid pH value reaches consistent and≤1.3.
3. a kind of D382 type resin acidic as claimed in claim 1 resolves technique, it is characterised in that in step 4, and parsing operation is selected and resolved agent is the hydrochloric acid solution of 3.5g/L.
4. one D382 type resin acidic as claimed in claim 1 resolves technique, it is characterised in that in step 6, after qualifying liquid precipitation is complete, is initially charged 1.5 times of slurry volume clear water and carries out clear water precipitation, after drained supernatant, then enters filter press operation acquisition product.
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| CN103846081B true CN103846081B (en) | 2016-06-29 |
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| CN106702184A (en) * | 2016-12-30 | 2017-05-24 | 新疆中核天山铀业有限公司 | Clear water desorption process of alkalescence anion resin |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4242097A (en) * | 1979-03-05 | 1980-12-30 | Dionex Corporation | Method and apparatus for quantitative analysis of weakly ionized anions or cations |
| CN101195862A (en) * | 2007-12-20 | 2008-06-11 | 金川集团有限公司 | Method for purifying and cadmium removing from nickel and cobalt solution |
| CN101224436A (en) * | 2007-09-25 | 2008-07-23 | 张剑秋 | Ion exchange resin regeneration method |
| CN102219258A (en) * | 2010-04-14 | 2011-10-19 | 湖南荣宏钼业材料股份有限公司 | Method for extracting molybdenum from waste materials in ammonium molybdate production field |
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- 2012-12-06 CN CN201210518105.7A patent/CN103846081B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4242097A (en) * | 1979-03-05 | 1980-12-30 | Dionex Corporation | Method and apparatus for quantitative analysis of weakly ionized anions or cations |
| CN101224436A (en) * | 2007-09-25 | 2008-07-23 | 张剑秋 | Ion exchange resin regeneration method |
| CN101195862A (en) * | 2007-12-20 | 2008-06-11 | 金川集团有限公司 | Method for purifying and cadmium removing from nickel and cobalt solution |
| CN102219258A (en) * | 2010-04-14 | 2011-10-19 | 湖南荣宏钼业材料股份有限公司 | Method for extracting molybdenum from waste materials in ammonium molybdate production field |
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