CN201825993U - Continuous ion exchange device for extracting gallium in Bayer mother liquid - Google Patents
Continuous ion exchange device for extracting gallium in Bayer mother liquid Download PDFInfo
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- CN201825993U CN201825993U CN2010205832213U CN201020583221U CN201825993U CN 201825993 U CN201825993 U CN 201825993U CN 2010205832213 U CN2010205832213 U CN 2010205832213U CN 201020583221 U CN201020583221 U CN 201020583221U CN 201825993 U CN201825993 U CN 201825993U
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Abstract
The utility model discloses a continuous ion exchange device and a method for extracting gallium in Bayer mother liquid, wherein the device comprises resin, resin columns for loading the resin, a main discharging pipe communicated with the upper ends of the resin columns, and a main feeding pipe communicated on the lower ends of the resin columns; the resin columns comprise at least four groups of resin column groups in series; the main feeding pipe comprises a main Bayer mother liquid feeding pipe, a main washing feeding pipe, a main leaching feeding pipe and a main transformational feeding pipe; the main discharging pipe comprises a main Bayer mother liquid feeding pipe, a main washing feeding pipe, a main leaching feeding pipe and a main transformational feeding pipe; each group of resin column is provided with a feeding branch pipe communicated with the main feeding pipe and a discharging branch pipe communicated with the main discharging pipe respectively; and each feeding branch pipe and each discharging branch pipe are respectively provided with a control valve for cooperatively controlling alternation among all the groups of the resin column groups so as to realize ion exchange, washing, leaching and transformation process of resin. The method has the advantages that the equipment is simple, the operation is convenient and the automation level is high.
Description
Technical field
The utility model relates to a kind of continuous ionic switch, is specifically related to a kind of continuous ionic switch that extracts gallium from the Bayer mother liquor.
Background technology
Gallium is a kind of dissipated metal, and important purposes is arranged in semi-conductor industry, along with development of semiconductor, the demand of gallium is increased day by day.The source rareness of gallium, its product come from the by product of aluminium industry etc. more.Resin method is produced gallium, has become the main path that extracts gallium from the alumina producing flow process at present.In traditional fixed-bed process,, make solution increasing, thereby reduce throughput, have a strong impact on production because of resistance because the aluminium hydroxide seston constantly deposits in resin.What therefore the gallium of resin method production at present process adopted is the packed moving bed technology mostly, moving bed technique can reach the purpose of extracting gallium preferably, but in the process of extracting, between processes such as absorption, washing, parsing, regeneration, shift continually owing to resin, cause that resin itself wearing and tearing are big, resin imbalance etc. between the easily efflorescence, complicated operating process, each process, directly have influence on the life cycle of resin and the stability of production process.Comparatively Xian Jin ISEP technology can more fully effectively utilize resin, greatly reduces the waste discharge amount, but very high to the reliability requirement of system, and the cost of operation is also much higher for fixed bed and moving-bed.
Chinese patent CN101067165A discloses the ion exchange method of extracting gallium from the alumina producing flow process: adopt two kinds of different ion-exchange units to extract gallium from alumina producing, that is: utilize packed moving bed to adsorb, utilize the full adverse current mixed bed ion exchange process of fixed bed drip washing, full two associatings of washing and making the transition, said method comprising the steps of: packed moving bed is adopted in (1) absorption, and the concentration of tail washings gallium is 70-110mg/L; (2) full washing adopted single fixed bed, the clear water washing; (3) the clear water washing is adopted in rinsing, and superficial linear velocity is 6-13m/s; (4) drip washing of a plurality of fixed bed counter flow in series is adopted in drip washing; (5) adopt transition a plurality of fixed bed counter flow in series clear water to make the transition; (6) resin successively in absorption, full wash, rinsing, drip washing, establishing in each of transition periodically move.The packed moving bed method of using in this patent, resin needs constantly to carry in system, resin is broken serious, the resin loses rate was about 10-20% in 1 month, need constantly to increase resin and guarantee that whole resin bed has certain exchange capacity, and the cost proportion of resin accounts for more than 50% of overall running cost in the process of extracting gallium.The packed moving bed that uses in this patented method is satisfied and is washed device structure complexity such as tower, rinsing tower, and the specification disunity is given to manufacture and design and brought certain trouble.
The utility model content
To exist resin to destroy when extracting gallium serious so the technical problem that the utility model solves is existing packed moving bed ion exchange method, the defective of complex process, for solving this defective, the utility model provides a kind of continuous ionic switch that extracts gallium from the Bayer mother liquor, this device has simple in structure, the advantage that production cost is low.
For realizing above-mentioned utility model purpose, the continuous ionic switch that from the Bayer mother liquor, extracts gallium that the utility model provides, a kind of continuous ionic switch that from the Bayer mother liquor, extracts gallium, comprise resin, be used to load a plurality of resin columns of resin, the discharge header pipe that is communicated with resin column upper end and the charging house steward who is communicated with the resin column lower end, it is characterized in that:
Be connected in series successively by series pipe between the described resin column, and form the resin column group that at least four groups are moved synchronously in turn;
Described charging house steward comprises Bayer mother liquor charging house steward, wash feed house steward, drip washing charging house steward and charging transition house steward, described discharge header pipe comprises Bayer mother liquor discharge header pipe, washing discharge header pipe, drip washing discharge header pipe and the discharge header pipe that makes the transition, and is respectively equipped with feed-inputing branched pipe that is communicated with the charging house steward and the discharging arm that is communicated with described discharge header pipe on described every group of resin column group;
Described feed-inputing branched pipe comprises Bayer mother liquor feed-inputing branched pipe, wash feed arm, drip washing feed-inputing branched pipe and the feed-inputing branched pipe that makes the transition, and described Bayer mother liquor feed-inputing branched pipe, wash feed arm, drip washing feed-inputing branched pipe and the feed-inputing branched pipe that makes the transition are communicated with described Bayer mother liquor charging house steward, wash feed house steward, drip washing charging house steward and charging transition house steward are corresponding one by one;
Described discharging arm comprises Bayer mother liquor discharging arm, washing discharging arm, drip washing discharging arm and discharging transition arm, and described Bayer mother liquor discharging arm, washing discharging arm, drip washing discharging arm and discharging transition arm are with described Bayer mother liquor discharge header pipe, washing discharge header pipe, drip washing discharge header pipe and transition corresponding one by one connection of discharge header pipe;
Be respectively equipped with control valve on described each feed-inputing branched pipe, discharging arm and the series pipe, be used for periodically controlling each resin column group realizes ion-exchange, washing, drip washing and resin in different time sections transformation process.
Form four groups of resin column groups by the series pipe series connection between the described resin column, described four groups of resin column groups are respectively adsorption resin column group, washing resin post group, drip washing resin column group and the resin column group that makes the transition, wherein,
The series connection resin column quantity of described adsorption resin column group is at least 3;
The series connection resin column quantity of described washing resin post group is at least 1;
The series connection resin column quantity of described drip washing resin column group is at least 3;
Described transition, the series connection resin column quantity of resin column group was at least 1.
Form five groups of resin column groups by the series pipe series connection between the described resin column, described five groups of resin column groups are respectively adsorption resin column group, full resin column group, rinsing resin column group, drip washing resin column group and the resin column group that makes the transition of washing, wherein,
The series connection resin column quantity of described adsorption resin column group is at least 3;
Described full series connection resin column quantity of washing the resin column group is at least 1;
The series connection resin column quantity of described rinsing resin column group is at least 1;
The series connection resin column quantity of described drip washing resin column group is at least 3;
Described transition, the series connection resin column quantity of resin column group was at least 2;
Described wash feed house steward comprises full wash charging house steward and rinsing charging house steward, and described washing discharge header pipe comprises full material house steward and the rinsing discharge header pipe of washing out;
Described wash feed arm comprises full wash feed-inputing branched pipe and rinsing feed-inputing branched pipe;
Described washing discharging arm comprises full material arm and the rinsing discharging arm of washing out.
Described resin is the strong acid and strong base resin, strong acid weak base resin, weak acid highly basic resin, a kind of in the weak acid and weak base resin.
Described control valve is magnetic valve or pneumavalve, and described control valve is used for the keying of the control valve on the described feed-inputing branched pipe of sequential control, discharging arm and the series pipe by the PLC time variable control.
A kind of continuous ionic switching method of utilizing said apparatus to extract gallium from the Bayer mother liquor comprises the steps:
Step 1: a plurality of resin columns are connected in series successively forms placed in-line four groups of resin column groups, promptly adsorption resin column group, washing resin post group, drip washing resin column group and transition the resin column group;
Step 2: with Bayer mother liquor feed liquid, washings, leacheate and transition liquid enter respectively in the resin column group of setting quantity separately, finish the transformation process of gallium ion exchange, resin column washing, resin column drip washing and resin synchronously;
Step 3: after last one-period is finished, realize that by switching control valve on the resin column four groups of resin column groups carry out new combination in turn between a plurality of resin columns;
Step 4: with Bayer mother liquor feed liquid, washings, leacheate and transition liquid enter respectively in four groups of resin column groups of the next cycle after reconfiguring, finish the transformation process of gallium ion exchange, resin column washing, resin column drip washing and the resin of next cycle synchronously.
Mother liquor feed liquid, washings, leacheate and transition liquid respectively from resin column bottom feed liquor, behind the resin of flowing through in the top of resin column fluid.
The superficial linear velocity of described mother liquor feed liquid is 10-30m/h, feed time 60-1200min;
The superficial linear velocity of described washings is at 5-15m/h, feed time 60-1200min;
The superficial linear velocity of described leacheate is at 5-12m/h, feed time 60-1200min;
Described transition, the superficial linear velocity of liquid was at 5-12m/h, feed time 60-1200min;
Wherein said mother liquor feed liquid, washings, leacheate are identical with the feed time of liquid transition, and the time that the described control valve cycle switches is more than or equal to feed time.
Described mother liquor feed liquid is that temperature is the mother liquor that produces in 30-40 ℃ the use alumina producing Bayer process process, gallium content: 10-500mg/l wherein, alumina content: 50-120g/l, sodium oxide content: 100-200g/l;
The washings and the liquid that makes the transition are H
2O;
Leacheate Na
2The mixed solution of S and NaOH, wherein the concentration of Na2S is 20-30g/L, the concentration of NaOH is 2.0-3.0mol/L.
Another kind utilizes said apparatus to extract the continuous ionic switching method of gallium from the Bayer mother liquor, comprises the steps:
A plurality of resin columns are connected in series successively forms placed in-line five groups of resin column groups, promptly the adsorption resin column group, full wash resin column group, rinsing resin column group, drip washing resin column group and transition the resin column group;
With Bayer mother liquor feed liquid, full washing lotion, rinsing liquid, leacheate and transition liquid enter respectively in the resin column group of setting quantity separately, finish synchronously that gallium ion exchange, resin column are fullly washed, the transformation process of resin column rinsing, resin column drip washing and resin; After last one-period is finished, realize that by switching control valve on the resin column five groups of resin column groups carry out new combination in turn between a plurality of resin columns; With Bayer mother liquor feed liquid, full washing lotion, rinsing liquid, leacheate and transition liquid enter respectively in five groups of resin column groups of the next cycle after reconfiguring, finish synchronously that gallium ion exchange, the resin column of next cycle fullly washed, the transformation process of resin column rinsing, resin column drip washing and resin.
Mother liquor feed liquid, full washing lotion, rinsing liquid, leacheate and transition liquid respectively from resin column bottom feed liquor, behind the resin of flowing through in the top of resin column fluid.
The superficial linear velocity of described mother liquor feed liquid is 10-30m/h, feed time 60-1200min;
The superficial linear velocity of described full washing lotion is 6-15m/h, feed time 60-1200min;
The superficial linear velocity of described rinsing liquid is 5-15m/h, feed time 60-1200min;
The superficial linear velocity of described leacheate is 5-12m/h, feed time 60-1200min;
Described transition, the superficial linear velocity of liquid was 5-12m/h, feed time 60-1200min;
Wherein said mother liquor feed liquid, full washing lotion, rinsing liquid, leacheate are identical with the feed time of liquid transition, and the time that the described control valve cycle switches is more than or equal to feed time.
Described mother liquor feed liquid is that temperature is the mother liquor that produces in 30-40 ℃ the use alumina producing Bayer process process, gallium content: 10-500mg/l wherein, alumina content: 50-120g/l, sodium oxide content: 100-200g/l;
Full washing lotion, rinsing liquid and transition liquid be H
20;
Leacheate Na
2The mixed solution of S and NaOH, wherein Na
2The concentration of S is 20-30g/L, and the concentration of NaOH is 2.0-3.0mol/L.
The utility model extracts gallium from the Bayer mother liquor continuous ionic exchange process adopts the continuous ionic exchange system, resin position in the continuous ionic switch is motionless, switching by the automatic control system valve, make the different zones resin realize absorption simultaneously, satisfy and wash rinsing, drip washing, transition, autocontrol valve is pneumavalve or magnetic valve, adopts the PLC program controlled mode.
Particularly, method of the present utility model can realize by following technique measures:
The utility model extracts gallium from the Bayer mother liquor continuous ionic exchange process adopts the continuous ionic exchange system, and resin position in the continuous ionic switch is motionless, by the switching of automatic control system valve, make the different zones resin realize absorption simultaneously, satisfy and wash rinsing, drip washing, transition.Said method comprising the steps of:
Adsorption zone: the operation of n1 post, feed liquid enters from the resin column bottom, and top goes out.Superficial linear velocity is controlled at 10-30m/h
The full district of washing: the operation of n2 post, clear water enters from the resin column bottom, and top goes out.Superficial linear velocity is controlled at 6-15m/h
The rinsing district: the operation of n3 post, clear water enters from the resin column bottom, and top goes out.Superficial linear velocity is controlled at 5-15m/h
The drip washing district: the operation of n4 post, eluent enters from the resin column bottom, and top goes out.Superficial linear velocity is controlled at 5-12m/h
Distinguish transition: the operation of n5 post, and clear water enters from the resin column bottom, and top goes out.Superficial linear velocity is controlled at 5-12m/h
Total n resin column in the system, in the section, n1 post is positioned at adsorption zone at one time, and n2 post is positioned to satisfy washes the district, and n3 post is positioned at the rinsing district, and n4 post is positioned at the drip washing district, and n5 post is positioned at district's transition.Each resin region periodically changes.Wherein, n=n1+n2+n3+n4+n5, n1 〉=3, n2 〉=1, n3 〉=1, n4 〉=3, n5 〉=2
Adsorption zone process described in the utility model may further comprise the steps: n1 post series operation, the Bayer mother liquor by the resin column bottom enter fully exchange with resin after, go out from first step resin column is suitable for reading, enter from second stage resin column end opening more afterwards, process is carried out according to this, until going out, turn back to the alumina producing operation as tail washings from n1 resin column is suitable for reading.
The full district's process of washing described in the utility model may further comprise the steps: clear water enters from the resin column bottom, and mother liquor residual in the resin is slowly ejected and turns back in the mother liquor tank, and maximum possible makes does not have mother liquor residual in the resin.
Rinsing district process described in the utility model may further comprise the steps: clear water enters from the resin column bottom, and top goes out.The flushing of big flow makes resin obtain loose fully and launches, and takes the resin chips of partial crushing out of.
Drip washing district process described in the utility model may further comprise the steps: n4 post series operation, leacheate from first step resin column end opening enter fully exchange with resin after, go out from first step resin column is suitable for reading, enter from second stage resin column end opening more afterwards, process is carried out according to this, is used for follow-up oxidization electrolysis operation as qualifying liquid until suitable for reading from n4 resin column after going out.
District's transition described in the utility model may further comprise the steps: n5 post series operation, clear water enters from the resin column bottom, with eluent flushing remaining in the resin fully, after resin makes the transition fully, continues on for the adsorption process of adsorption zone.
More than absorption, full washing, rinsing, drip washing, transformation process is carried out synchronously, and periodically carries out the switching of valve.Each resin column is finished above institute in steps through the circulation in a week.
Method of the present utility model adopts continuous ion exchange apparatus targetedly, adsorption process is adopted the counter flow in series absorption mode, the resin that adsorbs after saturated enters the full resin column group territory of washing, and new transition, good resin was proceeded absorption as the last step of adsorption process.Improve the utilization ratio of resin, avoided the course of conveying mechanical damage of resin.Series model is adopted in drip washing, has reduced the consumption of eluent, has improved qualifying liquid concentration, has increased productivity effect.Finish to compare with existing packed moving bed and ISEP, have that equipment is simple, equipment design unified, easy to operate and characteristics that level of automation is high.
Description of drawings
Fig. 1 is the process flow sheet of continuous ionic exchange process of the present utility model;
Fig. 2 is the process flow sheet of the another kind of continuous ionic exchange process of the utility model;
Fig. 3 is the continuous ionic exchange process device of Fig. 1;
Fig. 4 is a PLC time variable control wiring diagram of the present utility model.
Among the figure: 1. Bayer mother liquor discharging arm 2. rinsing discharging arms 3. discharging transition arms
4. the full material arm 5. drip washing qualifying liquid discharging arms 6. Bayer mother liquor feed-inputing branched pipes that wash out
7. rinsing feed-inputing branched pipe 8. feed-inputing branched pipe transition 9. full feed-inputing branched pipes of washing
10. drip washing feed-inputing branched pipe 11. pneumavalves/magnetic valve 12. resin columns
13. the Bayer mother liquor discharge header pipe 14. full material house steward 15. rinsing discharge header pipe that wash out
16. drip washing qualifying liquid discharge header pipe discharge header pipe 17. transition 18. charging transition house stewards
19. drip washing charging house steward 20. rinsing charging house stewards 21. satisfy and wash the charging house steward
22. Bayer mother liquor charging house steward 23. seriess pipe.
Embodiment
The utility model is further described below in conjunction with embodiment, but does not limit the utility model.
As Figure 1-3, the continuous ionic switch that from the Bayer mother liquor, extracts gallium of the present utility model, comprise resin, be used to load a plurality of resin columns of resin, the discharge header pipe that is communicated with resin column upper end and the charging house steward who is communicated with the resin column lower end, form at least four group resin column groups by the series pipe series connection between the resin column;
The charging house steward comprises Bayer mother liquor charging house steward, wash feed house steward, drip washing charging house steward and charging transition house steward, discharge header pipe comprises Bayer mother liquor discharge header pipe, washing discharge header pipe, drip washing discharge header pipe and the discharge header pipe that makes the transition, and is respectively equipped with feed-inputing branched pipe that is communicated with the charging house steward and the discharging arm that is communicated with discharge header pipe on every group of resin column group;
Feed-inputing branched pipe comprises Bayer mother liquor feed-inputing branched pipe, wash feed arm, drip washing feed-inputing branched pipe and the feed-inputing branched pipe that makes the transition, and Bayer mother liquor feed-inputing branched pipe, wash feed arm, drip washing feed-inputing branched pipe and the feed-inputing branched pipe that makes the transition are communicated with described Bayer mother liquor charging house steward, wash feed house steward, drip washing charging house steward and charging transition house steward are corresponding one by one;
The discharging arm comprises Bayer mother liquor discharging arm, washing discharging arm, drip washing discharging arm and discharging transition arm, and Bayer mother liquor discharging arm, washing discharging arm, drip washing discharging arm and discharging transition arm are with Bayer mother liquor discharge header pipe, washing discharge header pipe, drip washing discharge header pipe and transition corresponding one by one connection of discharge header pipe;
Be respectively equipped with control valve on each feed-inputing branched pipe, discharging arm and the series pipe, be used to coordinate to control the transformation process of realizing ion-exchange, washing, drip washing and resin between each resin column group synchronously.
Resin is the strong acid and strong base resin, strong acid weak base resin, weak acid highly basic resin, a kind of in the weak acid and weak base resin.
Control valve is magnetic valve or pneumavalve, and described control valve is used for the switching of the control valve on each pipeline of sequential control by the PLC time variable control.
As shown in Figure 4, all corresponding technical process controls are carried out relevant operation by the CPU in the PLC system.Each pillar operating unit is divided into absorption, satisfies and washes rinsing, five steps of drip washing and transition are continuous, continuous into mother liquor (full washing lotion, the rinsing liquid that be divided into again of each step, the leacheate and the liquid that makes the transition) start (closing), valve open (closing), transmitter starts (cutting out) three and column unit.At a time, all pillars are satisfied and are washed in operation absorption, rinsing, a certain step in the drip washing and the step that makes the transition.As being example with the 1# post, give 1# post absorption instruction by CPU, this moment, transmitter obtained giving the feed valve gating signal, the charging valve open after the order of CPU.After preset time, CPU gives 1# post absorption END instruction, and this moment, transmitter obtained giving the feed valve gating signal after the order of CPU, the charging valve closes, absorption finishes, and with this signal feedback to CPU.This moment, CPU gave that the 1# post is full washes instruction, and this moment, transmitter obtained advancing to satisfy after the order of CPU washing lotion valve signal, and the washing lotion valve open advances to satisfy.After preset time, CPU gives that the 1# post is full washes END instruction, this moment, transmitter obtained advancing rinsing liquid valve signal after the order of CPU, advance the rinsing liquid valve open, after preset time, CPU gives 1# post rinsing END instruction, and this moment, transmitter obtained advancing leacheate valve signal after the order of CPU, advance the leacheate valve open, rinsing finishes.After preset time, CPU gives 1# post drip washing END instruction, this moment, transmitter obtained advancing fluid valve signal transition after the order of CPU, and the fluid valve that advances to make the transition is opened, and drip washing finishes, after preset time, CPU gives END instruction 1# post transition, and this moment, transmitter obtained advancing fluid valve signal transition after the order of CPU, and the fluid valve that advances to make the transition is closed, finish transition, and the 1# post begins next algorithm.The control principle of other posts is identical with the 1# post with step.
Embodiment 1
As shown in Figure 2, the continuous ionic switch that from the Bayer mother liquor, extracts gallium that the utility model provides, comprise resin, be used to load a plurality of resin columns of resin, reach the charging house steward who is communicated with the resin column lower end with the discharge header pipe that is communicated with on the resin column, a plurality of resin columns are connected in series successively forms placed in-line four groups of resin column groups, promptly adsorption resin column group, washing resin post group, drip washing resin column group and transition the resin column group;
The charging house steward comprises Bayer mother liquor charging house steward, wash feed house steward, drip washing charging house steward and charging transition house steward, discharge header pipe comprises Bayer mother liquor discharge header pipe, washing discharge header pipe, drip washing discharge header pipe and the discharge header pipe that makes the transition, and is respectively equipped with feed-inputing branched pipe that is communicated with the charging house steward and the discharging arm that is communicated with described discharge header pipe on every group of resin column group;
Feed-inputing branched pipe comprises Bayer mother liquor feed-inputing branched pipe, wash feed arm, drip washing feed-inputing branched pipe and the feed-inputing branched pipe that makes the transition, and Bayer mother liquor feed-inputing branched pipe, wash feed arm, drip washing feed-inputing branched pipe and the feed-inputing branched pipe that makes the transition are communicated with Bayer mother liquor charging house steward, wash feed house steward, drip washing charging house steward and charging transition house steward are corresponding one by one;
The discharging arm comprises Bayer mother liquor discharging arm, washing discharging arm, drip washing discharging arm and discharging transition arm, and described Bayer mother liquor discharging arm, washing discharging arm, drip washing discharging arm and discharging transition arm are with Bayer mother liquor discharge header pipe, washing discharge header pipe, drip washing discharge header pipe and transition corresponding one by one connection of discharge header pipe;
Be respectively equipped with control valve on each feed-inputing branched pipe, discharging arm and the series pipe, be used to coordinate to control the transformation process of realizing ion-exchange, washing, drip washing and resin between each resin column group synchronously.
Wherein, the series connection resin column quantity of adsorption resin column group is at least 3; The series connection resin column quantity of washing resin post group is at least 1; The series connection resin column quantity of drip washing resin column group is at least 3; Transition, the series connection resin column quantity of resin column group was at least 1;
The utility model provides a kind of continuous ionic switching method of extracting gallium from the Bayer mother liquor, referring to Fig. 2, comprises the steps:
Step 1: a plurality of resin columns are connected in series successively forms four groups of resin column groups, promptly adsorption resin column group, washing resin post group, drip washing resin column group and transition the resin column group;
Step 2: with Bayer mother liquor feed liquid, washings, leacheate and transition liquid enter respectively in the resin column group of setting quantity separately, finish the transformation process of gallium ion exchange, resin column washing, resin column drip washing and resin synchronously;
Step 3: after last one-period is finished, realize that by switching control valve on the resin column four groups of resin column groups carry out new combination in turn between a plurality of resin columns;
Step 4: with Bayer mother liquor feed liquid, washings, leacheate and transition liquid enter respectively in four groups of resin column groups of the next cycle after reconfiguring, finish the transformation process of gallium ion exchange, resin column washing, resin column drip washing and the resin of next cycle synchronously.
Mother liquor feed liquid in the above-mentioned steps, washings, leacheate and transition liquid respectively from resin column bottom feed liquor, behind the resin of flowing through in the top of resin column fluid.
Wherein: the polymeric adsorbent that is loaded in the resin column is a SEPLITE LSC-600 resin (Xi'an Lanxiao Sci-Tech Co., Ltd.), and the superficial linear velocity of mother liquor feed liquid is 10-30m/h, feed time 60-1200min;
The superficial linear velocity of washings is at 5-15m/h, feed time 60-1200min;
The superficial linear velocity of leacheate is at 5-12m/h, feed time 60-1200min;
Transition, the superficial linear velocity of liquid was at 5-12m/h, feed time 60-1200min;
Mother liquor feed liquid, washings, leacheate are identical with the feed time of liquid transition, and the time that the PLC time variable control by-pass valve control cycle switches is more than or equal to feed time.
Described mother liquor feed liquid is that temperature is the mother liquor that produces in 30-40 ℃ the use alumina producing Bayer process process, gallium content: 10-500mg/l wherein, alumina content: 50-120g/l, sodium oxide content: 100-200g/l;
The washings and the liquid that makes the transition are H
2O;
Leacheate Na
2The mixed solution of S and NaOH, wherein the concentration of Na2S is 20-30g/L, the concentration of NaOH is 2.0-3.0mol/L.The extraction yield of gallium is 93%.
As shown in Figure 1, the continuous ionic switch that from the Bayer mother liquor, extracts gallium that the utility model provides, comprise resin, be used to load a plurality of resin columns of resin, reach the charging house steward who is communicated with the resin column lower end with the discharge header pipe that is communicated with on the resin column, a plurality of resin columns are connected in series successively forms placed in-line five groups of resin column groups, promptly the adsorption resin column group, full wash resin column group, rinsing resin column group, drip washing resin column group and transition the resin column group;
The charging house steward comprises Bayer mother liquor charging house steward, satisfies and wash charging house steward, rinsing charging house steward, drip washing charging house steward and charging transition house steward, discharge header pipe comprises Bayer mother liquor discharge header pipe, full material house steward, rinsing discharge header pipe, drip washing discharge header pipe and the discharge header pipe that makes the transition of washing out, and is respectively equipped with feed-inputing branched pipe that is communicated with the charging house steward and the discharging arm that is communicated with described discharge header pipe on every group of resin column group;
Feed-inputing branched pipe comprise Bayer mother liquor feed-inputing branched pipe, full wash feed-inputing branched pipe, rinsing feed-inputing branched pipe, drip washing feed-inputing branched pipe and transition feed-inputing branched pipe, Bayer mother liquor feed-inputing branched pipe, full wash feed-inputing branched pipe, rinsing feed-inputing branched pipe, drip washing feed-inputing branched pipe and transition feed-inputing branched pipe with Bayer mother liquor charging house steward, fullly wash that charging house steward, rinsing charging house steward, drip washing charging house steward and charging transition house steward are corresponding one by one to be communicated with;
The discharging arm comprises Bayer mother liquor discharging arm, full material arm, rinsing discharging arm, drip washing discharging arm and the discharging transition arm of washing out, and described Bayer mother liquor discharging arm, full material arm, rinsing discharging arm, drip washing discharging arm and the discharging transition arm of washing out are with Bayer mother liquor discharge header pipe, full washing out material house steward, rinsing discharge header pipe, drip washing discharge header pipe and transition corresponding one by one connection of discharge header pipe;
Be respectively equipped with control valve on each feed-inputing branched pipe, discharging arm and the series pipe, be used to coordinate to control realize ion-exchange between each resin column group synchronously, fullly wash, the transformation process of rinsing, drip washing and resin.
Wherein, the series connection resin column quantity of adsorption resin column group is at least 3, can guarantee the maximum adsorption of gallium in the mother liquor, improves the utilization ratio of resin and mother liquor.Increase progressively absorption step by step and make three first step resin columns in series connection adsorbed state that before going out the adsorption resin column group, reaches capacity;
Full series connection resin column quantity of washing the resin column group is at least 1, and clear water enters from the resin column bottom, and mother liquor residual in the resin is slowly ejected and turns back in the mother liquor tank, and maximum possible makes does not have mother liquor residual in the resin;
The resin column quantity of rinsing resin column group is at least 1, also can adopt the plural serial stage operational mode, and clear water enters from the resin column bottom, and top goes out.The flushing of big flow makes resin obtain loose fully and launches, and takes the resin chips of partial crushing out of;
The series connection resin column quantity of drip washing resin column group is at least 3, leacheate from first step resin column end opening enter fully exchange with resin after, go out from first step resin column is suitable for reading, enter from second stage resin column end opening more afterwards, process is carried out according to this, is used for follow-up oxidization electrolysis operation as qualifying liquid until suitable for reading from the last step resin column after going out.At least 3 post series operation patterns can guarantee that the eluent concentration that drip washing goes out increases progressively step by step, reduce the usage quantity of leacheate and at utmost improve the concentration of gallium in the qualifying liquid;
Transition, the series connection resin column quantity of resin column group was at least 2, clear water enters from the resin column bottom, with eluent flushing remaining in the resin fully, after resin makes the transition fully, continue on for the adsorption process of adsorption resin column group, at least the two-stage series connection operational mode can continue on for second stage resin column from first step resin column effusive transition of liquid, and the consumption that reduces agent transition reduces total system running cost.
The utility model also provides a kind of continuous ionic switching method of extracting gallium from the Bayer mother liquor, comprises the steps:
Step 1: a plurality of resin columns are connected in series successively forms placed in-line five groups of resin column groups, promptly the adsorption resin column group, full wash resin column group, rinsing resin column group, drip washing resin column group and transition the resin column group;
Step 2: with Bayer mother liquor feed liquid, full washing lotion, rinsing liquid, leacheate and transition liquid enter respectively in the resin column group of setting quantity separately, finish synchronously that gallium ion exchange, resin column are fullly washed, the transformation process of resin column rinsing, resin column drip washing and resin;
Step 3: after last one-period is finished, realize that by switching control valve on the resin column five groups of resin column groups carry out new combination in turn between a plurality of resin columns;
Step 4: with Bayer mother liquor feed liquid, full washing lotion, rinsing liquid, leacheate and transition liquid enter respectively in five groups of resin column groups of the next cycle after reconfiguring, finish synchronously that gallium ion exchange, the resin column of next cycle fullly washed, the transformation process of resin column rinsing, resin column drip washing and resin.
Wherein: the polymeric adsorbent that is loaded in the resin column is a SEPLITE LSC-600 resin (Xi'an Lanxiao Sci-Tech Co., Ltd.), and the superficial linear velocity of mother liquor feed liquid is 10-30m/h, feed time 60-1200min;
The superficial linear velocity of full washing lotion is 6-15m/h, feed time 60-1200min;
The superficial linear velocity of rinsing liquid is 5-15m/h, feed time 60-1200min;
The superficial linear velocity of leacheate is 5-12m/h, feed time 60-1200min;
Transition, the superficial linear velocity of liquid was 5-12m/h, feed time 60-1200min;
Mother liquor feed liquid, full washing lotion, rinsing liquid, leacheate are identical with the feed time of liquid transition.
The time that the PLC time variable control valve cycle switches is more than or equal to feed time.
Described mother liquor feed liquid is that temperature is the mother liquor that produces in 30-40 ℃ the use alumina producing Bayer process process, gallium content: 10-500mg/l wherein, alumina content: 50-120g/l, sodium oxide content: 100-200g/l;
The washings and the liquid that makes the transition are H
2O;
Leacheate Na
2The mixed solution of S and NaOH, wherein Na
2The concentration of S is 20-30g/L, and the concentration of NaOH is 2.0-3.0mol/L, and the extraction yield of gallium is 91.3%.
The structure of the continuous ionic switch of extraction gallium is with embodiment 2 from the Bayer mother liquor, and wherein the series connection resin column quantity of adsorption resin column group is 3; Full series connection resin column quantity of washing the resin column group is 1; The series connection resin column quantity of rinsing resin column group is 1; The series connection resin column quantity of drip washing resin column group is 3; Transition, the series connection resin column quantity of resin column group was 2.The polymeric adsorbent that is loaded in the resin column is a SEPLITE LSC-600 resin (Xi'an Lanxiao Sci-Tech Co., Ltd.).
Wherein: feed time is 60min, the superficial linear velocity of mother liquor feed liquid is 30m/h, the superficial linear velocity of full washing lotion is at 15m/h, the superficial linear velocity of rinsing liquid is at 15m/h, the superficial linear velocity of leacheate is at 12m/h, transition, the superficial linear velocity of liquid was at 12m/h, and be 180min switching time in control valve cycle.
Described mother liquor feed liquid is that temperature is the mother liquor that produces in 30 ℃ the use alumina producing Bayer process process, gallium content: 500mg/l wherein, alumina content: 120g/l, sodium oxide content: 200g/l.
Full washing lotion, rinsing liquid and transition liquid be H2O;
The mixed solution of leacheate Na2S and NaOH, wherein the concentration of Na2S is 30g/L, the concentration of NaOH is 3.0mol/L.The extraction yield of gallium is 94.2%.
Concrete operations are as follows: resin column take the to connect operator scheme of continous way
Table 1 resin column different zones function step table
Annotate: the numbering of the digitized representation resin column in the table 1.
With the 1st cycle in the table 1 be example, each resin column that is indicated among Fig. 1 is in the period 1 zone, that is:
1# post: rinsing resin column group 2# post: the full resin column group of washing
3#, 4#, the 5# post: adsorption resin column group 6#, the 7# post: the resin column group makes the transition
8#, 9#, 10#, 11# post: drip washing resin column group
1# post: rinsing resin column group.The 1# post is to enter rinsing resin column group after a last switching cycle is in the switching of resin by control valve of washing the resin column group of satisfying.There has not been remaining mother liquor in the resin after satiety is washed.Clear water enters from end opening, outflow suitable for reading.Superficial linear velocity 15m/h.The qualified resin of rinsing after rinsing resin column group waits for that whole switching time, 180min finished, enters next cycle.
2# post: the full resin column group of washing.The 2# post is to enter the full resin column group of washing after first step resin column that a last switching cycle is in the adsorption resin column group has adsorbed the switching of saturated resin by control valve fully.Through remaining mother liquor in a large number in the resin after the absorption.Clear water enters from end opening, outflow suitable for reading.Superficial linear velocity: 15m/h.
3#, 4#, 5# post: adsorption resin column group.3#, 4#, 5# post series connection, mother liquor enters from 3# post end opening, suitable for readingly goes out.Enter from 4# post end opening afterwards, suitable for readingly go out.5# post end opening enters, and suitable for readingly goes out to be discharged to the alumina producing operation again.Charging 3# post end opening mother liquor gallium concentration 240-300mg/l, discharging 5# tail washings gallium suitable for reading concentration 70-90mg/l.3#, 4#, mother liquid concentration is successively decreasing gradually in the 5# post, and mother liquid concentration is the highest in the 3# post.
Successively decrease gradually through absorption back mother liquid concentration.Superficial linear velocity: 30m/h.
8#, 9#, 10#, 11# post: drip washing resin column group.Enter the resin process level Four drip washing of drip washing resin column group, the concentration of the efficient of assurance drip washing and the qualifying liquid gallium of last step 11# column outlet.The Gallium solution of the lower concentration that 8# drip washing goes out enters in the 9# post and continues drip washing, and the concentration of gallium is improved in the eluent concentration.Through the lasting increase of concentration of 10# post gallium, behind the 11# post, the concentration of gallium reaches maximum value again.Guarantee resin through after the drip washing of level Four, when the 8# post will leave drip washing resin column group, the suction gallium amount of resin was a Schwellenwert at once.Superficial linear velocity: 12m/h.
6#, the 7# post: the resin column group makes the transition.Enter resin column group transition through the resin after the drip washing, clear water enters from the end opening of 6# post, suitable for readingly goes out.Enter from 7# post end opening again, suitable for readingly go out.Clear water is fully used, and is directly used in the preparation leacheate from liquid transition of 7# column outlet.Superficial linear velocity: 12m/h.
Embodiment 4
With embodiment 3 different be: the employing feed time is 180min, the superficial linear velocity of mother liquor feed liquid is 20m/h, the superficial linear velocity of full washing lotion is at 10m/h, the superficial linear velocity of rinsing liquid is at 12m/h, the superficial linear velocity of leacheate is at 8m/h, transition, the superficial linear velocity of liquid was at 8m/h, and be 180min switching time in control valve cycle.
The mother liquor feed liquid is that temperature is the mother liquor that produces in 40 ℃ the use alumina producing Bayer process process, gallium content: 400mg/l wherein, alumina content: 100g/l, sodium oxide content: 150g/l.
Leacheate Na
2The mixed solution of S and NaOH, wherein Na
2The concentration of S is 30g/L, and the concentration of NaOH is 3.0mol/L.The extraction yield of gallium is 89.3%.
Embodiment 5
With embodiment 3 different be: the polymeric adsorbent that is loaded in the resin column is a SEPLITE LSC-600 resin (Xi'an Lanxiao Sci-Tech Co., Ltd.), the employing feed time is 500min, the superficial linear velocity of mother liquor feed liquid is 20m/h, the superficial linear velocity of full washing lotion is at 10m/h, the superficial linear velocity of rinsing liquid is at 10m/h, the superficial linear velocity of leacheate is at 10m/h, and transition, the superficial linear velocity of liquid was at 10m/h, and be 600min switching time in control valve cycle.
The mother liquor feed liquid is that temperature is the mother liquor that produces in 40 ℃ the use alumina producing Bayer process process, gallium content: 300mg/l wherein, alumina content: 80g/l, sodium oxide content: 120g/l.
Leacheate Na
2The mixed solution of S and NaOH, wherein Na
2The concentration of S is 15g/L, and the concentration of NaOH is 2.0mol/L.The extraction yield of gallium is 90.5%.
With embodiment 3 different be: the polymeric adsorbent that is loaded in the resin column is a SEPLITE LSC-600 resin (Xi'an Lanxiao Sci-Tech Co., Ltd.), the employing feed time is 1200min, the superficial linear velocity of mother liquor feed liquid is 10m/h, the superficial linear velocity of full washing lotion is at 6m/h, the superficial linear velocity of rinsing liquid is at 5m/h, the superficial linear velocity of leacheate is at 5m/h, and transition, the superficial linear velocity of liquid was at 5m/h, and be 1200min switching time in control valve cycle.
The mother liquor feed liquid is that temperature is the mother liquor that produces in 40 ℃ the use alumina producing Bayer process process, gallium content: 10mg/l wherein, alumina content: 50g/l, sodium oxide content: 100g/l.
Leacheate Na
2The mixed solution of S and NaOH, wherein Na
2The concentration of S is 20g/L, and the concentration of NaOH is 2.0mol/L.The extraction yield of gallium is 88.3%.
Embodiment 7
With embodiment 3 different be: the polymeric adsorbent that is loaded in the resin column is a SEPLITE LSC-600 resin (Xi'an Lanxiao Sci-Tech Co., Ltd.), and the series connection resin column quantity of adsorption resin column group is 4; Full series connection resin column quantity of washing the resin column group is 2; The series connection resin column quantity of rinsing resin column group is 2; The series connection resin column quantity of drip washing resin column group is 5; Transition, the series connection resin column quantity of resin column group was 3.
The mother liquor feed liquid is that temperature is the mother liquor that produces in 40 ℃ the use alumina producing Bayer process process, gallium content: 50mg/l wherein, alumina content: 80g/l, sodium oxide content: 100g/l.
Leacheate Na
2The mixed solution of S and NaOH, wherein Na
2The concentration of S is 20g/L, and the concentration of NaOH is 2.0mol/L.The extraction yield of gallium is 92.1%.
The structure of the continuous ionic switch of extraction gallium is with embodiment 1 from the Bayer mother liquor, and wherein, the series connection resin column quantity of adsorption resin column group is 3; The series connection resin column quantity of washing resin post group is 1; The series connection resin column quantity of drip washing resin column group is 3; Transition, the series connection resin column quantity of resin column group was 1; The polymeric adsorbent that is loaded in the resin column is a SEPLITE LSC-600 resin (Xi'an Lanxiao Sci-Tech Co., Ltd.)
Wherein: feed time is 60min, the superficial linear velocity of mother liquor feed liquid is 30m/h, the superficial linear velocity of full washing lotion is at 15m/h, the superficial linear velocity of rinsing liquid is at 15m/h, the superficial linear velocity of leacheate is at 12m/h, transition, the superficial linear velocity of liquid was at 12m/h, and be 180min switching time in control valve cycle.
Described mother liquor feed liquid is that temperature is the mother liquor that produces in 30 ℃ the use alumina producing Bayer process process, gallium content: 500mg/l wherein, alumina content: 120g/l, sodium oxide content: 200g/l.
Full washing lotion, rinsing liquid and transition liquid be H
2O;
Leacheate Na
2The mixed solution of S and NaOH, wherein the concentration of Na2S is 30g/L, the concentration of NaOH is 3.0mol/L.The extraction yield of gallium is 89.7%.
Concrete operations such as table 2: a plurality of resin columns take to connect operator scheme of continous way.
Table 2 resin column different zones function step table
Annotate: the numbering of the digitized representation resin column in the table 1.
Embodiment 9
With embodiment 8 different be: the polymeric adsorbent that is loaded in the resin column is a SEPLITE LSC-600 resin (Xi'an Lanxiao Sci-Tech Co., Ltd.), the employing feed time is 180min, the superficial linear velocity of mother liquor feed liquid is 30m/h, the superficial linear velocity of full washing lotion is at 15m/h, the superficial linear velocity of rinsing liquid is at 15m/h, the superficial linear velocity of leacheate is at 12m/h, and transition, the superficial linear velocity of liquid was at 12m/h, and be 180min switching time in control valve cycle.
The mother liquor feed liquid is that temperature is the mother liquor that produces in 30 ℃ the use alumina producing Bayer process process, gallium content: 100mg/l wherein, alumina content: 50g/l, sodium oxide content: 100g/l.
Leacheate Na
2The mixed solution of S and NaOH, wherein Na
2The concentration of S is 20g/L, and the concentration of NaOH is 2.0mol/L.The extraction yield of gallium is 93.3%.
With embodiment 8 different be: the polymeric adsorbent that is loaded in the resin column is a SEPLITE LSC-600 resin (Xi'an Lanxiao Sci-Tech Co., Ltd.), the employing feed time is 500min, the superficial linear velocity of mother liquor feed liquid is 25m/h, the superficial linear velocity of washings is at 12m/h, the superficial linear velocity of leacheate is at 10m/h, transition, the superficial linear velocity of liquid was at 10m/h, and be 600min switching time in control valve cycle.
The mother liquor feed liquid is that temperature is the mother liquor that produces in 40 ℃ the use alumina producing Bayer process process, gallium content: 200mg/l wherein, alumina content: 100g/l, sodium oxide content: 120g/l.
Leacheate Na
2The mixed solution of S and NaOH, wherein Na
2The concentration of S is 25g/L, and the concentration of NaOH is 2.0mol/L.The extraction yield of gallium is 88.6%.
With embodiment 8 different be: the polymeric adsorbent that is loaded in the resin column is a SEPLITE LSC-600 resin (Xi'an Lanxiao Sci-Tech Co., Ltd.), the employing feed time is 1000min, the superficial linear velocity of mother liquor feed liquid is 15m/h, the superficial linear velocity of washings is at 9m/h, the superficial linear velocity of leacheate is at 7m/h, transition, the superficial linear velocity of liquid was at 7m/h, and be 1000min switching time in control valve cycle.
The mother liquor feed liquid is that temperature is the mother liquor that produces in 40 ℃ the use alumina producing Bayer process process, gallium content: 100mg/l wherein, alumina content: 50g/l, sodium oxide content: 100g/l.
Leacheate Na
2The mixed solution of S and NaOH, wherein Na
2The concentration of S is 20g/L, and the concentration of NaOH is 2.0mol/L.The extraction yield of gallium is 92.2%.
With embodiment 8 different be: the polymeric adsorbent that is loaded in the resin column is a SEPLITE LSC-600 resin (Xi'an Lanxiao Sci-Tech Co., Ltd.), the employing feed time is 1200min, the superficial linear velocity of mother liquor feed liquid is 10m/h, the superficial linear velocity of washings is at 15m/h, the superficial linear velocity of leacheate is at 5m/h, transition, the superficial linear velocity of liquid was at 5m/h, and be 1200min switching time in control valve cycle.
The mother liquor feed liquid is that temperature is the mother liquor that produces in 30 ℃ the use alumina producing Bayer process process, gallium content: 100mg/l wherein, alumina content: 50g/l, sodium oxide content: 100g/l.
Leacheate Na
2The mixed solution of S and NaOH, wherein Na
2The concentration of S is 20g/L, and the concentration of NaOH is 2.0mol/L.The extraction yield of gallium is 87.4%.
Claims (5)
1. continuous ionic switch that extracts gallium from the Bayer mother liquor comprises resin, is used to load a plurality of resin columns of resin, the discharge header pipe that is communicated with the resin column upper end and the charging house steward who is communicated with the resin column lower end, it is characterized in that:
Be connected in series successively by series pipe between the described resin column, and form the resin column group that at least four groups are moved synchronously in turn;
Described charging house steward comprises Bayer mother liquor charging house steward, wash feed house steward, drip washing charging house steward and charging transition house steward, described discharge header pipe comprises Bayer mother liquor discharge header pipe, washing discharge header pipe, drip washing discharge header pipe and the discharge header pipe that makes the transition, and is respectively equipped with feed-inputing branched pipe that is communicated with the charging house steward and the discharging arm that is communicated with described discharge header pipe on described every group of resin column group;
Described feed-inputing branched pipe comprises Bayer mother liquor feed-inputing branched pipe, wash feed arm, drip washing feed-inputing branched pipe and the feed-inputing branched pipe that makes the transition, and described Bayer mother liquor feed-inputing branched pipe, wash feed arm, drip washing feed-inputing branched pipe and the feed-inputing branched pipe that makes the transition are communicated with described Bayer mother liquor charging house steward, wash feed house steward, drip washing charging house steward and charging transition house steward are corresponding one by one;
Described discharging arm comprises Bayer mother liquor discharging arm, washing discharging arm, drip washing discharging arm and discharging transition arm, and described Bayer mother liquor discharging arm, washing discharging arm, drip washing discharging arm and discharging transition arm are with described Bayer mother liquor discharge header pipe, washing discharge header pipe, drip washing discharge header pipe and transition corresponding one by one connection of discharge header pipe;
Be respectively equipped with control valve on described each feed-inputing branched pipe, discharging arm and the series pipe, be used for periodically controlling each resin column group realizes ion-exchange, washing, drip washing and resin in different time sections transformation process.
2. the continuous ionic switch that extracts gallium from the Bayer mother liquor according to claim 1 is characterized in that:
Form four groups of resin column groups by the series pipe series connection between the described resin column, described four groups of resin column groups are respectively adsorption resin column group, washing resin post group, drip washing resin column group and the resin column group that makes the transition, wherein,
The series connection resin column quantity of described adsorption resin column group is at least 3;
The series connection resin column quantity of described washing resin post group is at least 1;
The series connection resin column quantity of described drip washing resin column group is at least 3;
Described transition, the series connection resin column quantity of resin column group was at least 1.
3. the continuous ionic switch that extracts gallium from the Bayer mother liquor according to claim 1 is characterized in that:
Form five groups of resin column groups by the series pipe series connection between the described resin column, described five groups of resin column groups are respectively adsorption resin column group, full resin column group, rinsing resin column group, drip washing resin column group and the resin column group that makes the transition of washing, wherein,
The series connection resin column quantity of described adsorption resin column group is at least 3;
Described full series connection resin column quantity of washing the resin column group is at least 1;
The series connection resin column quantity of described rinsing resin column group is at least 1;
The series connection resin column quantity of described drip washing resin column group is at least 3;
Described transition, the series connection resin column quantity of resin column group was at least 2;
Described wash feed house steward comprises full wash charging house steward and rinsing charging house steward, and described washing discharge header pipe comprises full material house steward and the rinsing discharge header pipe of washing out;
Described wash feed arm comprises full wash feed-inputing branched pipe and rinsing feed-inputing branched pipe;
Described washing discharging arm comprises full material arm and the rinsing discharging arm of washing out.
4. according to the arbitrary described continuous ionic switch that from the Bayer mother liquor, extracts gallium of claim 1-3, it is characterized in that:
Described resin is the strong acid and strong base resin, strong acid weak base resin, weak acid highly basic resin, a kind of in the weak acid and weak base resin.
5. according to the arbitrary described continuous ionic switch that from the Bayer mother liquor, extracts gallium of claim 1-3, it is characterized in that:
Described control valve is magnetic valve or pneumavalve, and described control valve is used for the keying of the control valve on the described feed-inputing branched pipe of sequential control, discharging arm and the series pipe by the PLC time variable control.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010205832213U CN201825993U (en) | 2010-10-29 | 2010-10-29 | Continuous ion exchange device for extracting gallium in Bayer mother liquid |
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|---|---|---|---|
| CN2010205832213U CN201825993U (en) | 2010-10-29 | 2010-10-29 | Continuous ion exchange device for extracting gallium in Bayer mother liquid |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101962713A (en) * | 2010-10-29 | 2011-02-02 | 西安蓝晓科技有限公司 | Continuous ion exchange device and method for extracting gallium from Bayer mother solution |
| CN109179467A (en) * | 2018-09-30 | 2019-01-11 | 中铝山东有限公司 | A method of gallium is removed to the low pregnant Bayer process liquor of concentration containing gallium |
-
2010
- 2010-10-29 CN CN2010205832213U patent/CN201825993U/en not_active Expired - Lifetime
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101962713A (en) * | 2010-10-29 | 2011-02-02 | 西安蓝晓科技有限公司 | Continuous ion exchange device and method for extracting gallium from Bayer mother solution |
| CN101962713B (en) * | 2010-10-29 | 2012-11-07 | 西安蓝晓科技新材料股份有限公司 | Continuous ion exchange device and method for extracting gallium from Bayer mother solution |
| CN109179467A (en) * | 2018-09-30 | 2019-01-11 | 中铝山东有限公司 | A method of gallium is removed to the low pregnant Bayer process liquor of concentration containing gallium |
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Address after: High tech Zone technology two road 710075 Shaanxi city of Xi'an province No. 72 Chak tower 4 Patentee after: Sunresin New Materials Co., Ltd., Xi'an Address before: High tech Zone technology two road 710075 Shaanxi city of Xi'an province No. 72 Chak tower 4 Patentee before: Xian Sunresin Technology Co., Ltd. |
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