CN1298029A - Integral equipment and technological process of adsorption, desorption and electrolysis of gold leachate - Google Patents
Integral equipment and technological process of adsorption, desorption and electrolysis of gold leachate Download PDFInfo
- Publication number
- CN1298029A CN1298029A CN99117408A CN99117408A CN1298029A CN 1298029 A CN1298029 A CN 1298029A CN 99117408 A CN99117408 A CN 99117408A CN 99117408 A CN99117408 A CN 99117408A CN 1298029 A CN1298029 A CN 1298029A
- Authority
- CN
- China
- Prior art keywords
- tower
- desorb
- switching tube
- solution
- desorption
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Images
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
Landscapes
- Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)
- Electrolytic Production Of Metals (AREA)
Abstract
The integral gold producing equipment and process including adsorption, desorption and electrolysis in mine has no need of repeated loading, unloading and transportation of active carbon in and between adsorption tower and desorption tower, and the lean electrolyte may be reused in soaking operation to recover its gold, sodium cyanide and sodium hydroxide. Therefore, the present invention has raised gold extracting rate and lowered production cost. The present invention has an adsorption rate over 99 %, a desorption rate over 98 %, an electrolysis rate over 99 % and a desorption-electrolysis period as short as 10-12 hr.
Description
Low-grade gold dump leaching technology from the beginning of the seventies since the U.S. comes out, become one of main means that gold in the world produces at present.China began one's study and progressively applies from the eighties, and the dump leaching scale develops into 10 tons by kiloton.The Application and Development of dump leaching technology plays huge pushing effect to the development and use of China's low-grade gold resource.But, up at present in gold heaping leaching is produced, mainly be in adsorption tower, to adsorb with gac, and in desorption tower, gold loaded carbon desorption two is overlapped the operations of independent device sectional type, contain the charcoal absorption of golden rich solution through adsorption tower from what the ore deposit dump leaching went out, after treating that year golden charcoal absorption reaches capacity, from adsorption tower, draw off and carry golden charcoal, be transported near the special desorb factory (desorb factory generally all build from mining area far away cities and towns) far away from the mine, the desorption tower of packing into carries out desorb, the golden liquid of separating sucking-off is sent into after filtering and is carried out electrolysis in the electrolyzer, on negative electrode, obtain gold mud, take off and be smelted into ingot after gold mud is handled, because adsorption operation is to carry out in the adsorption tower of mine, and the desorb operation is to finish in the desorption tower in the desorb factory far away of mining area, adsorption and desorption two covering devices are independent fully, this sectional type process operation can produce following problems inevitably:
(1) gac draws off, transports, reinstalls desorption tower from adsorption tower; Draw off from desorption tower again after the desorb, transport the dump leaching field adsorption tower of packing into again back and adsorb.In this circulated repeatedly, gac especially carried the loss that being scattered of golden charcoal can be caused gold because of loading and unloading and transport the loss of being scattered that causes charcoal repeatedly.Carry the efflorescence that golden charcoal is squeezed, rubs and causes charcoal in transit.Absorption principle according to gac is known, carbon surface (especially edges and corners) is to the adsorptive capacity maximum of gold, and when being squeezed and rub, the easiest efflorescence again of carbon surface and corner angle, its consequence is not only the adsorption activity and the work-ing life of having reduced gac, and in desorption process, these secondary powdered carbons also do not obtain good desorb and just flow into electrolyzer with solution, not only caused golden deadweight loss, and pollute electrolytic solution, influence electrolysis effectiveness, can cause electrolysis to stop because of powdered carbon too much causes electric pole short circuit in the time of seriously.
For the influence of eliminating powdered carbon and the loss of reclaiming powdered carbon minimizing gold, the mine that has has been set up before desorb and has been sieved matting together, the powdered carbon that cleans out can reclaim most of through sedimentation and filtration, but still have the fine floating powdered carbon of part to be difficult to whole recovery, increased production cost again owing to set up a procedure simultaneously.
(2) owing to carry a golden charcoal and transport to the desorb workshop and just can return use through after the desorb, and dump leaching absorption in mine is carried out continuously, and this has enough to meet the need with regard to forcing the mine to be had to prepare a large amount of gacs.The mine that has is not owing to set up the desorb workshop, its year, golden charcoal must be entrusted outer processing desorb, the time of return of charcoal is just longer, even just there is not the degold charcoal can return use then at all, 1 year, the dump leaching mine of 10000 tons of milling of ores generally need prepare 5 tons of gacs, the production current assets overstocks, and has seriously increased the input amount of production capital.
(3) can not obtain desorb timely owing to carry golden charcoal, the gold that the mine produces also just can not in time become cash, and is slow to the turnover of funds that makes production period.Entrust the mine of outer processing desorb for those, the gold of current year's production just can become cash often when producing fast the end, and it is extremely low that this just causes the required fund of production period all to keep production, working capital turnover rate by the mine cash call.
(4) discharging of lean electrolyte is a hard nut to crack concerning desorbing electrolytic factory all the time.At first, in order to reclaim the gold in the lean electrolyte, desorb factory must set up lean solution adsorption operation again, as if the oxide compound that will reclaim in the solution, must increase equipment through the lean solution after the absorption again; If directly discharging also must be passed through purifying treatment.
(5) entrust outer processing desorb, when a year golden charcoal mixing is taken a sample, can cause once damaged again and the efflorescence loss, and often being prone to difference and dispute in golden charcoal grade and the moisture determination carrying, this is that both Parties are all felt the something of having a headache, and not only time-consumingly takes great energy, but also expensive.Processing charges also is a no small number concerning the consigner simultaneously, generally accounts for the 15-20% of direct production cost.
(6) existing desorbing electrolytic technology all is to carry out under normal pressure, so can only be used for the mine, low altitude area.Though the existing high pressure desorption equipment of China comes out, owing to cost an arm and a leg, general dump leaching mine is difficult to bear.
The objective of the invention is to: solve the problem that occurs in the above-mentioned gold heaping leaching production, for providing a kind of, the mine can reduce the gold loss effectively, reduce production costs, speed up capital turnover improves the business economic benefit, integrates the gold leachate adsorption-desorption electrolysis integrated apparatus and the production technique of absorption, desorb, electrolytic functional, this covering device and technology are directly used in the mine, can adsorb the limit desorb in the limit, the limit electrolysis is worked continuously, and reaches the purpose that goes out the electrolysis bronze in the mine with regard to the energy direct production.
The objective of the invention is that following technical scheme realizes by implementing:
Gold leachate adsorption-desorption electrolysis integrated apparatus is made of adsorption-desorption tower, well heater, electrolyzer, filtration steam separator, cooling tower, distillation basin, stationary tank and the adsorption system pipeline and the desorbing electrolytic system pipeline that connect these equipment unit.
Adsorption-desorption tower:, can in a tower, realize two kinds of functions of adsorption and desorption as the adsorption-desorption double-duty tower.This tower is made up of tower body, top cover and base.Top cover is fixed on the tower body top by ring flange, and base is fixed on the tower body bottom by ring flange, thereby is connected to form an integral body.Top cover is provided with that lean solution goes out pipe and stripping liquid goes out to manage, and tensimeter is housed, the base bottom is provided with rich solution inlet pipe and stripping liquid inlet pipe, between two ring flanges between tower body and top cover, and between the two method dishes between tower body and base screen cloth is set, and unit temp meter on the tower body, tower body top is provided with the active carbon material feeding mouth, the tower body bottom is provided with the gac discharge port at position, flange top, and in the peripheral packing of tower body thermal insulation layer is arranged.The present invention is provided with multistage identical adsorption-desorption double-duty tower.
Well heater: in conjunction with production scene, mine practical situation, the present invention can adopt the well heater of three kinds of type of heating, a kind ofly is electrically heated, and adopting electric heating tube is that heating source heats to stripping liquid, reaches the required temperature of desorb; Second kind is the diesel oil heating, this type of heating is to allow diesel oil heat thermal oil by combustion engine, after being heated, heats to stripping liquid again thermal oil, reach the temperature that desorb needs, the third mode is for to come to heat-conducting oil heating with coal combustion, allow the heat-conducting oil heating stripping liquid again, reach the required temperature of desorb, a kind of of these three kinds of type of heating can be selected according to the local energy resources situation in the production mine.
Electrolyzer: owing to the stripping liquid temperature that enters electrolyzer is higher, generally at 90-100 ℃, the common plastics thermal stability is not high, so the cell vessel in this dress adopts the PP plastic plate of 120 ℃ of abilities to make.Positive plate in the electrolyzer is a stainless steel plate, and negative electrode is to have thin stainless steel wool as the hairline, and this steel wool is contained in the negative electrode box, in interleave with stainless cathode bar.
Filter steam separator: material is the charcoal steel, divides inside and outside two-layerly, and internal layer is provided with 100 purpose filter pore, is provided with 100 order stainless steel guards filtering the steam separator upper end, and guard is above to be the material filling type separation column.
Piping system of the present invention includes adsorption system pipeline and desorption system pipeline.
The adsorption system pipeline is responsible for by rich solution, the rich solution inlet pipe that connects tower separately and rich solution switching tube, lean solution between rich solution is responsible for are responsible for, are connected the lean solution of tower separately and go out pipe and the lean solution lean solution arm between being responsible for, and the absorption switch pipeline that connects between the rich solution switching tube of the lean solution arm of tower at the corresponding levels and subordinate's tower constitutes.
The desorbing electrolytic system pipeline is responsible for by the desorb feed liquor, the stripping liquid inlet pipe that connects tower at the corresponding levels is conciliate the desorb switching tube of inspiration liquid between being responsible for, the desorb fluid is responsible for, the stripping liquid that connects tower at the corresponding levels goes out pipe and conciliates the desorb fluid switching tube of sucking-off liquid between being responsible for, connect the desorb fluid person in charge at tailing column place and the filtration switching tube between filtration steam separator inlet, filter your the liquid transfer lime between steam separator liquid exit and electrolyzer inlet, lean electrolyte output tube between electrolyzer outlet and stationary tank, connect the stripping liquid outlet of stationary tank and the stripping liquid transfer lime that is connected with the stripping liquid inlet of well heater by valve and in-line pump, conciliate inspiration liquid with the outlet of well heater stripping liquid and be responsible for the heating desorption liquid output tube that is connected, connect the still tube that filters between steam separator and cooling tower, connect the distillation cooling fluid output tube between cooling tower liquid exit and distillation basin, and the dosing pipeline that connects between outlet of distillation basin and stationary tank constitutes.
The adsorption-desorption electrolysis process process that this device is finished is as follows:
1, dump leaching: contain the gold mine material with sodium cyanide (NaCN) dump leaching of 0.1-0.05% after will pulverizing, and, make the leach liquor pH value should remain on the 10-11 scope with the pH value of sodium hydroxide (NaOH) adjustment leach liquor.
2, dress tower: with 6-16 purpose gac, the towers at different levels of packing into successively, the gac in every tower generally accounts for the 70-80% of tower body.
3, absorption: dump leaching contains golden rich solution and enters the rich solution person in charge by the rich solution pond, enter Shou Ta by first tower rich solution switching tube, allow after the charcoal absorption gold, go out pipe by the lean solution of first cat head and enter the lean solution arm, and then enter in the secondary tower through the absorption switching tube and the rich solution switching tube of secondary tower, gac is once more after the ADSORPTION OF GOLD, go out pipe by the lean solution of secondary cat head and enter the lean solution arm, absorption switching tube and rich solution switching tube through three grades of towers enters three grades of towers again, by that analogy, contain the golden liquid towers at different levels by contacting successively, by the charcoal absorption gold, at last go out pipe and flow into lean solution through the lean solution arm and be responsible for, flow to again in the lean solution pond of dump leaching field, add medicament and return the ore deposit dump leaching again and go out gold by the lean solution of tailing column.After treating that first tower ADSORPTION OF GOLD reaches capacity, rich solution switching tube valve by it disconnects the rich solution inlet pipe, close the absorption switching tube of secondary tower, open the rich solution switching tube of secondary tower, allow the rich solution of rich solution in being responsible for enter the secondary tower through the rich solution switching tube of secondary tower, at this moment the secondary tower becomes the first tower of adsorption system, carries out above-mentioned sorption cycle process.
4, desorbing electrolytic: first tower and rich solution are responsible for disconnection, turn-off the lean solution arm, open with the desorb feed liquor and be responsible for desorb switching tube that links to each other and the desorb fluid switching tube that links to each other with the desorb fluid person in charge, the stripping liquid that has been heated to desorption temperature during the desorb feed liquor is responsible for enters Shou Ta and carries out desorb, desorb should be satisfied desorption condition in the tower: NaCN content is 2% in the stripping liquid, NaOH content is 1-2%, 100 ℃-120 ℃ of stripping liquid temperature, tower internal pressure 0.08-0.12MPa, liquid in the tower after desorb enters the desorb fluid through desorb fluid switching tube and is responsible for, switching tube enters the filtration steam separator after filtration then, golden liquid after the filtration enters electrolyzer through your liquid transfer lime and carries out electrolysis, bronze deposits on the steel wool of negative electrode, lean solution after the electrolysis enters stationary tank through the lean electrolyte output tube, lean electrolyte in the stationary tank pumps into the stripping liquid transfer lime through in-line pump and enters in the well heater, be heated to required desorption temperature, entering the desorb feed liquor by heating desorption liquid output tube then is responsible for, enter desorb in the tower through the desorb switching tube again, be recycled to desorb and so forth and finish.This tower entered adsorption system as the last tower of adsorption system again by tubing system after desorb finished, and so circulation is gone down, and reached the absorption of complete assembly limit, the limit desorb, and the limit electrolysis is in the purpose of dump leaching production scene, mine direct production electrolysis bronze.
Compare with desorption system and sectional type production technique with the adsorption system of forming by adsorption tower, desorption tower two cover independent device disconnected from each other, essential characteristic of the present invention is: adsorption tower and desorption tower do not adopt mutually independently two covering devices in the device, be equipped with on tower top cover that lean solution goes out pipe and stripping liquid goes out to manage but adopt, what rich solution inlet pipe and stripping liquid inlet pipe were housed on tower base not only has absorption but also have desorb, integrates the adsorption-desorption double-duty tower of two kinds of functions; Adsorption-desorption double-duty tower and supporting filtration steam separator, electrolyzer, stationary tank, well heater, cooling tower and piping system thereof have constituted the device that integrates absorption, desorb, electrolytic functional.
The present invention has following performance:
(1) adsorption rate is more than 99%, and desorption efficiency is more than 98%, and electrolyzing rate is more than 99%.
(2) desorbing electrolytic time weak point only needs 10-12 hour, uses conventional sectional type process then to need 48-60 hour.
(3) the present invention can realize limit absorption, limit desorb, limit electrolysis, output electrolysis bronze on the spot under various sea level elevations.
The invention has the advantages that:
(1) removes repeatedly loading and unloading and the long-distance transport of gac between adsorption tower and desorption tower from, reduced the loss and the efflorescence of year golden charcoal, saved trucking costs.
(2) because gac uses continuously, reduce overstocking and volume of the circular flow of gac in tower, reduced production current assets occupancy.
(3) mix the gold metallurgy stove can be directly the ingot of output acceptable quality at the scene, in time submit local bank, accelerated turnover of funds, reduced the cash input amount.
(4) lean electrolyte can directly return dump leaching operation use, fully recycles the gold in the lean solution, nacn, and sodium hydroxide further improves the rate of recovery of gold and has reduced production cost.
(5) the desorbing electrolytic cost is low, less than entrusting 1/4th of outer process cost.
The present invention has following accompanying drawing:
Fig. 1 is a gold leachate adsorption-desorption electrolysis integrated apparatus structural representation;
Fig. 2 is an adsorption-desorption double-duty tower structural representation;
Fig. 3 is the electric heater structural representation;
Fig. 4 is for filtering the steam separator structural representation;
Fig. 5 is the cell construction synoptic diagram, upward is the vertical profile front view, and the right side is a side-view, is vertical view down;
Fig. 6 is anode and a cathode junction composition in the electrolyzer, and the left side is upper and lower to be two kinds of shape anodes, in go up and to be negative electrode box side-view, in be negative electrode box vertical view down, upper right is negative electrode box front view, the bottom right is a cathode bar;
Fig. 7,8,9,10 is for originally installing pipes and valve signature figure.
Mark among the figure: 1 is the adsorption-desorption double-duty tower, 2 are the rich solution person in charge, and 3 is that lean solution is responsible for, and 4 is that the desorb feed liquor is responsible for, 5 are the desorb fluid person in charge, 6 is well heater, and 7 is in-line pump, and 8 for filtering steam separator, 9 is cooling tower, 10 is electrolyzer, and 11 are the distillation basin, and 12 is stationary tank, 13 is adsorption-desorption double-duty tower tower body, 14 is tower top cover, and 15 is tower base, and 16 is the rich solution inlet pipe, 17 go out pipe for lean solution, 18 is the stripping liquid inlet pipe, and 19 for stripping liquid goes out pipe, and 20 is upper flange, 21 is lower flange, 22 is screen cloth, and 23 is screen cloth, and 24 is the active carbon material feeding mouth, 25 is the gac discharge port, 26 is the tower body thermal insulation layer, and 27 is the well heater housing, and 28 is heating tube (electrothermal tube), 29 is well heater flange top cover, 30 is the heater heats liquid exit, and 31 are the heating liquid inlet, and 32 is heater support, 33 for filtering the steam separator outer wall, 34 is the internal layer strainer tube, and 35 is filter screen, and 36 is support, 37 for filtering the steam separator outlet, 38 is the material filling type separation column, and 39 is vapour outlet, and 40 for filtering the steam separator inlet, 41 is PP plastic electrobath wall, 42 is the clip type anode, and 43 is T-shaped formula anode, and 44 is negative electrode, 45 are the cell bath inlet, 46 are the cell bath outlet, and 47 are electrolyzer outlet down, and 48 is insulating barrier, 49 is the negative electrode box, 50 is cathode bar, tower rich solution switching tube headed by 51, and 52 is rich solution switching tube valve, 53 are the absorption switching tube, 54 are absorption switching tube valve, and 55 are the desorb switching tube, and 56 are desorb switching tube valve, 57 is the lean solution arm, 58 is lean solution arm valve, and 59 are secondary tower absorption switching tube, and 60 are absorption switching tube valve, 61 is the rich solution switching tube, 62 is rich solution switching tube valve, and 63 are the desorb switching tube, and 64 are desorb switching tube valve, 65 is the lean solution arm, 66 is lean solution arm valve, and 67 is three grades of tower absorption switching tubes, and 68 are absorption switching tube valve, 69 is the rich solution switching tube, 70 is rich solution switching tube valve, and 71 are the desorb switching tube, and 72 are desorb switching tube valve, 73 is the lean solution arm, 74 is lean solution arm valve, and 75 are level Four tower absorption switching tube, and 76 are absorption switching tube valve, 77 is the rich solution switching tube, 78 is rich solution switching tube valve, and 79 are desorb switching tube, 80 desorb switching tube valves, 81 is the lean solution arm, 82 is lean solution arm valve, and 83 are Pyatyi tower absorption switching tube, and 84 are absorption switching tube valve, 85 is the rich solution switching tube, 86 is rich solution switching tube valve, and 87 are the desorb switching tube, and 88 are desorb switching tube valve, 89 is the lean solution arm, 90 is lean solution arm valve, 91,93,95,97, tower headed by 99 difference, the secondary tower, three grades, level Four, the desorb fluid switching tube of Pyatyi tower, 92,94,96,98,100 are respectively the desorb fluid switching tube valve of towers at different levels, 101 for filtering switching tube, your liquid transfer lime 102 be, 103 is the lean electrolyte output tube, and 104 is the stripping liquid transfer lime, 105 is heating desorption liquid output tube, 106 is still tube, and 107 are distillation cooling fluid output tube, and 108 is liquid distribution pipe.
Further specify production process of the present invention below in conjunction with accompanying drawing embodiment:
Gold leachate adsorption-desorption electrolysis integrated apparatus of the present invention, its adsorption-desorption double-duty tower 5 the identical towers of contacting altogether.Screen cloth in the tower is 30 orders, and every tower is adorned 6-16 order gac 100kg, and tower body is surrounded by the spun-glass insulation layer, its lift of pump in the desorbing electrolytic system is 20 meters, and flow is 2.8-4 rice 3/ hour, and anode has 18 in the electrolyzer, 17 in negative electrode box, interior dress steel wool and cathode bar.
The absorbing process flow process is as follows:
One-level tower (first tower): close absorption opening-closing valve 54, absorption switching tube 53 is closed; Close desorb opening-closing valve 56, desorb switching tube 55 is closed; Close the desorb fluid opening-closing valve 92,94,96,98,100 of towers at different levels, the desorb fluid switching tube 91,93,95,97,99 of towers at different levels is closed, and closes lean solution arm valve 58, open rich solution opening-closing valve 52, rich solution switching tube 51 is opened, and is responsible for 2 with rich solution and connects, and rich solution enters Shou Ta.
The secondary tower: open absorption opening-closing valve 60, absorption switching tube 59 is opened, and closes rich solution opening-closing valve 62, and rich solution switching tube 61 is closed, and closes desorb opening-closing valve 64, and desorb switching tube 63 is closed, and closes lean solution arm valve 66.
Three grades of towers: open absorption opening-closing valve 68, absorption switching tube 67 is opened, and closes rich solution and opens.Closing valve 70, rich solution switching tube 69 is closed, and closes desorb opening-closing valve 72, and desorb switching tube 71 is closed, and closes lean solution arm valve 74.
Level Four tower (last tower): open absorption opening-closing valve 76, absorption switching tube 75 is opened, and closes rich solution opening-closing valve 78, rich solution switching tube 77 is closed, and closes desorb opening-closing valve 80, and desorb switching tube 79 is closed, open lean solution arm valve 82, lean solution arm 81 is responsible for 3 with lean solution and is connected.
Pyatyi tower: all valves (promptly 84,86,88,90) of closing this tower.
In first tower, gold is by a charcoal absorption part in the rich solution, contain golden liquid afterwards by the absorption switching tube 59 of lean solution arm 57 through the secondary tower, rich solution switching tube 61 enters in the secondary tower, gold is by one one of the charcoal absorption in the secondary tower, liquid is by its lean solution arm 65, absorption switching tube 67 through three grades of towers, rich solution switching tube 69 enters in three grades of towers, and the gold in the solution is once more by charcoal absorption, and liquid is by the absorption switching tube 75 of lean solution arm 73 through the level Four tower, rich solution switching tube 77 enters the level Four tower, gold in the solution is adsorbed for the last time, lean solution after the absorption flows into lean solutions by lean solution arm 81 and is responsible for 3, is admitted to the lean solution pond, adds to be admitted to the ore deposit heap again behind the medicine and to carry out dump leaching.
When the charcoal absorption gold in the first tower has reached when saturated, close first tower rich solution opening-closing valve 52, rich solution switching tube 51 is responsible for 2 with rich solution and is turn-offed, open desorb opening-closing valve 56, desorb switching tube 55 is opened with the desorb feed liquor and is responsible for 4 connections, opens desorb fluid opening-closing valve 92, desorb fluid switching tube 91 promptly is responsible for 5 with the desorb fluid and is connected, stripping liquid 100 ℃-120 ℃ of temperature in tower, pressure 0.08-0.12MPa, and contain NaCN
2%, contain under the NaOH1-2% condition, the gold of charcoal absorption is got off to enter in the stripping liquid by desorb, this liquid enters the desorb fluid through desorb fluid switching tube 91 and is responsible in 5, switching tube 101 enters in the filtration steam separator 8 after filtration again, your by liquid transfer lime 102 your liquid is sent in the electrolyzer 10 after filtration with after the vapor-liquid separation, lie prostrate at electrode voltage 2-4, under the dc electrolysis electric current 300-400 ampere condition, on the negative electrode steel wool, deposit bronze, lean solution after the electrolysis is sent in the stationary tank 12 by lean electrolyte output tube 103, is 20 meters by lift, and flow is a 2.8-4 rice
3/ hour in-line pump stripping liquid is pumped in the well heater 6 heating through stripping liquid transfer lime 104, make it to reach 100 ℃-120 ℃ desorption temperature, then by heating desorption liquid output tube 105, stripping liquid is sent into the desorb feed liquor be responsible for 4, enter first tower through desorb switching tube 55 again and continue desorb, so circulation is finished up to desorb.
The steam that fractionates out in filtering steam separator 8 enters cooling in the cooling tower 9 through still tube 106, cooling fluid is sent in the distillation basin 11 by distillation cooling fluid output tube 107, this liquid contains the alcohol of 70-80%, send in the stationary tank 12 desorb in tower is sent in heating of the lean electrolyte in the groove by liquid distribution pipe 108 as batching.
Carry out in the process in first tower desorb, close secondary tower absorption opening-closing valve 60, absorption switching tube 59 is closed, open rich solution opening-closing valve 62, rich solution switching tube 61 is opened with rich solution and is responsible for 2 connections, rich solution enters in the secondary tower, through 65, three grades of tower absorption of lean solution arm switching tube 67, rich solution switching tube 69 enters in three grades of towers, from lean solution arm 73, the level Four tower adsorbs switching tube 75 again, and rich solution switching tube 77 enters the level Four tower, enter absorption switching tube 83 and the absorption switching tube valve 84 of lean solution arm 81 again through the Pyatyi tower, close 82 valves simultaneously and make solution enter the Pyatyi tower, behind the charcoal absorption gold, lean solution enters the lean solution person in charge 3 by lean solution arm 89 and returns heap lean solution pond, ore deposit.At this moment, tower headed by the former secondary tower that is in adsorbed state becomes, former three grades of towers become the secondary tower, and former level Four tower becomes three grades of towers, and former Pyatyi tower becomes tailing column.After former secondary tower (tower headed by this moment) absorption reaches capacity, again it is isolated from adsorption system, carry out desorbing electrolytic.And former one-level tower is by opening valve 54, valve-off 56,90, allow the effusive lean solution of former Pyatyi tower (before being tailing column) by lean solution arm 89, absorption switching tube 53 and valve 54 enter this tower and adsorb, lean solution after the absorption is by lean solution arm 57, and valve 58 and lean solution are responsible for 3 and are returned heap lean solution pond, ore deposit.At this moment, former three grades of towers become the first tower of adsorption system again, and former level Four tower becomes the secondary tower, and former Pyatyi tower becomes three grades of towers, and former one-level tower becomes tailing column.So cyclical operation can reach limit absorption, limit desorb, limit electrolysis, and direct production goes out the electrolysis bronze in the production scene, mine.
Claims (4)
1, a kind of gold leachate absorption, desorb, electrolysis integrated apparatus, the desorbing electrolytic system that includes the adsorption system that is made of adsorption tower and pipeline thereof and be made of desorption tower and pipeline thereof and electrolyzer and pipeline thereof is characterized in that:
A, this device in, adsorption tower and desorption tower do not adopt mutually independently two covering devices, be equipped with on tower top cover (14) that lean solution goes out pipe (17) and stripping liquid goes out to manage (19) but adopt, what rich solution inlet pipe (16) and stripping liquid inlet pipe (18) were housed on tower base (15) not only has absorption but also have desorb, integrates absorption, the desorb double-duty tower of two kinds of functions.
B, adsorption-desorption double-duty tower and the filtration steam separator (8) that matches thereof, electrolyzer (10), stationary tank (12), well heater (6) and relevant piping system have constituted the device that integrates the adsorption-desorption electrolytic functional.
2, according to the described adsorption-desorption electrolysis of claim 1 integrated apparatus, it is characterized in that: the described piping system that matches with the adsorption-desorption double-duty tower includes: be responsible for (2), be connected the rich solution inlet pipe (16) of tower separately and rich solution and be responsible for rich solution switching tube, lean solution between (2) and be responsible for (3), be connected the adsorption system pipeline that the absorption switching tube between the rich solution switching tube that the lean solution of tower separately goes out lean solution arm, the lean solution arm that is connected tower at the corresponding levels and subordinate's tower between pipe (17) and the lean solution person in charge (3) is constituted by rich solution; Be responsible for (4) by the desorb feed liquor, the stripping liquid inlet pipe (18) that connects tower at the corresponding levels is conciliate inspiration liquid and is responsible for desorb switching tube between (4), the desorb fluid is responsible for (5), the stripping liquid that connects tower at the corresponding levels goes out pipe (19) and conciliates sucking-off liquid and be responsible for desorb fluid switching tube between (5), connect the desorb fluid person in charge (5) at tailing column place and the filtration switching tube (101) between filtration steam separator (8) inlet, filter your the liquid transfer lime (102) between steam separator (8) liquid exit and electrolyzer (10) inlet, lean electrolyte output tube (103) between electrolyzer (10) outlet and stationary tank (12), connect the stripping liquid outlet of stationary tank (12) and the stripping liquid transfer lime (104) that is connected with the stripping liquid inlet of well heater (6) by valve and in-line pump, conciliate inspiration liquid with the stripping liquid outlet of well heater (6) and be responsible for the heating desorption liquid output tube (105) that (4) are connected, connect the still tube (106) that filters between steam separator (8) and cooling tower (9), connect the liquid exit of cooling tower (9) and the distillation cooling fluid output tube (107) between distillation basin (11), and connect the desorbing electrolytic system pipeline that the liquid distribution pipe (108) between distillation basin (11) outlet and stationary tank (12) constitutes.
3, according to the described adsorption-desorption electrolysis of claim 2 integrated apparatus, it is characterized in that: the negative electrode (44) in the electrolyzer (10) is by negative electrode box (49), be loaded on the steel wool in the negative electrode box (49), the cathode bar (50) that inserts in negative electrode box (49) steel wool constitutes, positive plate in the electrolyzer (10) is made of clip type anode (42) and T-shaped formula anode (43), negative electrode (44) places between clip type anode (42) and the T-shaped formula anode (43), it is in proper order: first anode is a clip type, it is negative electrode thereafter, after the negative electrode is T-shaped formula anode, it again is negative electrode thereafter, after the negative electrode be again the clip type anode by that analogy, last negative electrode is the clip type anode afterwards.
4, according to the described adsorption-desorption electrolysis of claim 3 integrated apparatus, its employed technological process of production is:
The absorbing process flow process:
Dump leaching contains golden rich solution and enters the rich solution person in charge (2) by the rich solution pond, enter Shou Ta by first tower rich solution switching tube (51), allow after the charcoal absorption gold, go out pipe by the lean solution of first cat head and enter lean solution arm (57), and then enter in the secondary tower through the absorption switching tube (59) and the rich solution switching tube (61) of secondary tower, gac is once more after the ADSORPTION OF GOLD, go out pipe by the lean solution of secondary cat head and enter lean solution arm (65), absorption switching tube (67) and rich solution switching tube (69) through three grades of towers enters three grades of towers again, analogize in proper order, contain golden liquid and pass through the towers at different levels of polyphone successively by the charcoal absorption gold, lean solution by the level Four tower goes out pipe through lean solution arm (81) the inflow lean solution person in charge (3) at last, flow to again in the lean solution pond of dump leaching field, add medicament and return the ore deposit dump leaching again and go out gold.Treat that first tower ADSORPTION OF GOLD reaches capacity, close first tower rich solution inlet pipe (51), close the absorption switching tube (59) of secondary tower, open its rich solution switching tube (61), the golden rich solution that contains that allows rich solution be responsible in (2) enters the secondary tower through the rich solution switching tube (61) of secondary tower, this moment, the secondary tower became the first tower of adsorption system, simultaneously the 5th tower was sealed in absorption and carried out above-mentioned sorption cycle process.
The desorbing electrolytic technical process:
First tower and rich solution are responsible for (2) disconnection, close lean solution arm (57), open with the desorb feed liquor and be responsible for (4) the desorb switching tube (55) that links to each other and desorb fluid switching tube (91) that links to each other with the desorb fluid person in charge (5), the desorb feed liquor is responsible for the stripping liquid that has been heated to desorption temperature in (4) and is entered Shou Ta, carry out desorb, the condition that desorb should be satisfied in the tower: NaCN content is 2% in the stripping liquid, NaOH content is 1-2%, 100 ℃-120 ℃ of stripping liquid temperature, tower internal pressure 0.08-0.12MPa, liquid in the tower after the desorb enters the desorb fluid through desorb fluid switching tube (91) and is responsible for (5), switching tube (101) enters and filters steam separator (8) after filtration then, golden liquid after the filtration enters electrolyzer (10) through your liquid transfer lime (102) and carries out electrolysis, control negative and positive voltage across poles: 2-4 volt, electrolytic solution direct current 300-400 ampere, after your liquid enters electrolyzer, at first crossed clip type anode (42) top, going up aperture from negative electrode box (49) passes and enters the negative electrode box, fully contact with steel wool, deposition of gold is to steel wool, solution is flowed out by negative electrode box the opposing party aperture, enter next negative electrode box from the space between T-shaped formula anode and the cell vessel base plate again, solution contacts gold and deposits on the steel wool again with steel wool, solution is crossed clip type anode top again from the outflow of negative electrode box aperture and is entered next negative electrode again, by that analogy, after crossing from last clip type anode top, solution flows out electrolyzer, lean solution after the electrolysis enters stationary tank (12) through lean electrolyte output tube (103), lean electrolyte in the stationary tank (12) pumps into stripping liquid transfer lime (104) through in-line pump (17) and enters in the well heater (6), be heated to required desorption temperature, enter the desorb feed liquor by heating desorption liquid output tube (105) then and be responsible for (4), enter desorb in the tower through desorb switching tube (55) again, being recycled to desorb and so forth finishes, desorption time 10-12 hour, this tower entered adsorption system as the tailing column of adsorption system again by tubing system after desorb finished, so circulation is gone down, reach the absorption of complete assembly limit, the limit desorb, the limit electrolysis.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB991174089A CN1176231C (en) | 1999-12-02 | 1999-12-02 | Integral equipment and technological process of adsorption, desorption and electrolysis of gold leachate |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB991174089A CN1176231C (en) | 1999-12-02 | 1999-12-02 | Integral equipment and technological process of adsorption, desorption and electrolysis of gold leachate |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1298029A true CN1298029A (en) | 2001-06-06 |
| CN1176231C CN1176231C (en) | 2004-11-17 |
Family
ID=5280037
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB991174089A Expired - Fee Related CN1176231C (en) | 1999-12-02 | 1999-12-02 | Integral equipment and technological process of adsorption, desorption and electrolysis of gold leachate |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1176231C (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101012511B (en) * | 2007-02-12 | 2011-01-19 | 长春黄金研究院 | Method for eliminating calcium ion effect in gold ore bulk leaching by using descaling agent |
| CN102732721A (en) * | 2012-06-19 | 2012-10-17 | 广西地博矿业集团股份有限公司 | Closed circulation active carbon adsorption system |
| CN104087747A (en) * | 2014-04-21 | 2014-10-08 | 云南黄金矿业集团股份有限公司 | Method for desorbing valuable metals from gold loaded carbon |
| CN105112657A (en) * | 2015-05-25 | 2015-12-02 | 厦门紫金矿冶技术有限公司 | Gold extracting method with activated carbons |
-
1999
- 1999-12-02 CN CNB991174089A patent/CN1176231C/en not_active Expired - Fee Related
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101012511B (en) * | 2007-02-12 | 2011-01-19 | 长春黄金研究院 | Method for eliminating calcium ion effect in gold ore bulk leaching by using descaling agent |
| CN102732721A (en) * | 2012-06-19 | 2012-10-17 | 广西地博矿业集团股份有限公司 | Closed circulation active carbon adsorption system |
| CN104087747A (en) * | 2014-04-21 | 2014-10-08 | 云南黄金矿业集团股份有限公司 | Method for desorbing valuable metals from gold loaded carbon |
| CN104087747B (en) * | 2014-04-21 | 2017-07-14 | 云南黄金矿业集团股份有限公司 | The method that valuable metal is desorbed from gold loaded carbon |
| CN105112657A (en) * | 2015-05-25 | 2015-12-02 | 厦门紫金矿冶技术有限公司 | Gold extracting method with activated carbons |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1176231C (en) | 2004-11-17 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| WO2022033041A1 (en) | Extraction method for ion-adsorbed rare earths | |
| CN102167422B (en) | Recovery process of industrial waste acid | |
| CN104250046B (en) | A kind of nickel-contained wastewater treatment device and its processing method | |
| CN103582710A (en) | System and process for the continuous recovery of metals | |
| Liu et al. | Arsenic and cation metal removal from copper slag using a bipolar membrane electrodialysis system | |
| CN104817138A (en) | Electric flocculation device with inclined plate electrodes | |
| CN204625272U (en) | Be provided with the electric flocculation apparatus of swash plate electrode | |
| CN202519343U (en) | System for recovering copper from waste circuit board | |
| CN107285495A (en) | A kind of lithium ion battery production wastewater treatment device | |
| CN1176231C (en) | Integral equipment and technological process of adsorption, desorption and electrolysis of gold leachate | |
| CN205241426U (en) | A categorised recovery system for moving back tin waste liquid | |
| CN105712545A (en) | Copper-contained wastewater recycling system | |
| CN103408134B (en) | Anaerobic sludge bed reactor and method for treating organic waste water by using same | |
| CN109231379B (en) | Method for selectively recovering target ions from organic wastewater | |
| CN208667335U (en) | A kind of rare earth waste recycling RE waste water Integrated Processing Unit | |
| CN107235588A (en) | Produced Water In Oil-gas Fields, Ngi reinjection treatment method and equipment | |
| CN206396300U (en) | The dense backwater absorbent charcoal adsorber of cyanide carbon pulp technique | |
| CN101736159B (en) | Method for recovering gold from alkaline waste water | |
| CN100450941C (en) | Technical methd for treating mine wastewater by using membrane technology | |
| CN103397182B (en) | Method for efficiently recycling bismuth from monomer bismuth ore | |
| CN212293695U (en) | System for recovering gold, silver and copper from high-silver-copper gold-loaded carbon desorption electrolysis waste liquid | |
| CN212128272U (en) | Ion exchange system for recovering rhenium from rhenium-containing spraying liquid | |
| CN207827962U (en) | A kind of three phase separation unit, three phase separation module and modularization three phase separator | |
| CN206033340U (en) | Coal slime water treatment system | |
| CN105565544A (en) | Method for recycling nickel |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C02 | Deemed withdrawal of patent application after publication (patent law 2001) | ||
| WD01 | Invention patent application deemed withdrawn after publication | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C19 | Lapse of patent right due to non-payment of the annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |