CN103582710A - System and process for the continuous recovery of metals - Google Patents

Abstract

A system [100'] and process [100] for the continuous recovery of metals is disclosed. The system [100'] comprises a continuous acid wash system [10'], a holding tank [60], a continuous elution system [20'], a continuous electrowinning system [40'], a carbon regeneration system [30'], and a continuous carbon loading/adsorption system [70']. The systems and methods disclosed overcome the disadvantages associated with current systems and processes which utilize batch process steps and equipment designed for batch processes. The systems [10', 20', 30'] are each configured to receive a continuous inflow of a solution or slurry and deliver a continuous outflow of a solution or slurry, without interruptions which are common with conventional metal recovery systems [9000'].

Description

The system and method that is used for the continuous recovery of metal

Technical field

The present invention relates generally to mining and metallurgical refinement, and relates more specifically to for the solvent extraction of metal and the system and method for electrowinning.

Background technology

For this reason, two kinds of main method of existing cardinal principle concentrating and extracting for precious metal: zinc displacement and electrolytic deposition.Zinc displacement comprises the ore that contains precious metal (as, gold) is crushed and ground, and then ground ore mixed with water and caustic alkali cyanide solution.Resulting mud shape slurry is moved to subsider, wherein by gravity, thicker moved to bottom containing golden solid, and the first lighter mother liquor of Jiang Shui, gold and prussiate moves to top and removes for further processing.In separation, stir in leaching (leach) processing this is stirred and inflated containing golden solid, wherein oxygen reaction is to leach gold caustic-alkali aqueous and the prussiate that forms the second mother liquor.The second mother liquor is by core strainer, and it is separated remaining solid further.The first and second mother liquors are combined with zinc with by the deposition of gold dissolving out.Then can be by produced sludge gold enriched material melting to produce the gold bar of purifying.

Electrolytic deposition generally includes from electrolytic solution and extracts such as golden precious metal.First, in batch processing step, gac is mixed with mother liquor.This precious metal containing in this charcoal absorption mother liquor, thereby and " material containing " have this rare metal.Then residual by one after the other washing de-sludging to remove mineral three batch processing steps this material containing gac.First, material containing charcoal is moved to washing tank, and then this tank is filled with to dilute acid solutions.Then this washing tank is drained, and the dilute acid solutions after using is pumped and abandoned.Then this washing tank is filled to water to go remaining acid from the rinsing of material containing charcoal.In this process, water is by acidifying slightly.In the mode similar to dilute acid, the rinse water of used acidifying are slightly also emptying from washing tank, pump and abandon.Finally, tank is filled with caustic solution, and gac is washed in this caustic solution.Then used caustic solution is emptying from described tank, pump and abandon.Can again carry out optional final water rinse step, with rinse water or pH-neutral solution, fill this washing tank, residual from material containing charcoal rinsing caustic alkali, and follow the rinse water/solution from the emptying use of tank, make it can be pumped out to abandon.

After washing, from washing tank, remove material containing charcoal, and then add to the elution solution that comprises water, caustic alkali material and prussiate, to form elution solution/material containing charcoal slurry.This elution solution/material containing charcoal slurry is processed by wash-out, wherein use high temperature and pressure with by gold from material containing charcoal " re-leaching " to caustic alkali elution solution to form electrolyte solution.Then this electrolyte solution is moved to in batches electrolysis cells, its center line (as, netted) or plate negative electrode in electrolytic process, collects the golden enriched material depositing.After batch electrolytic deposition is processed, negative electrode is manually removed to clean from unit, thereby the golden enriched material of building up thereon can be removed and be prepared for melting from negative electrode.After clean, then negative electrode is manually reset in electrolysis cells, and the whole sequence of repetitive lots washing, wash-out and electrolytic deposition processing.Some negative electrodes (as, line cathode, due to its little space) be can not be reusable, and must after processing, reclaim, thereby increased overhead/running cost.

Show to the schematic property of Figure 27 common metal recycling 9000 as above.In routine batch charcoal load step 9700, activity or reactivate charcoal 9560 are suspended in mother liquor.This mother liquor substantially pads (for example,, by having approximately 0.5 to 1 pound of sodium cyanide by per ton, the solution of the enriched material of potassium cyanide or calcyanide drips or spray the mode of flushing) by the heap leaching that the cyanide solution infiltration of dilution contain to mineral ore by fragmentation and forms.Once gac from mother liquor adsorbed material requested (as, gold and silver, platinum, lead, copper, aluminium, platinum, uranium, cobalt, manganese), it becomes " material containing " charcoal 9570 and enters and is configured to as mentioned above the batch acid elution of material containing charcoal 9570 de-sludgings to process 9100.

Figure 28 shows the conventional example of pickling system 9100 ' in batches.Material containing charcoal 9570 enters pickling container 9120, and it receives dilute acid via pump 9132 from dilute acid tank 9140.Dilute acid overflow is caught by pond pump 9150 and this overflow is moved to neutral tank 9160.Can the content of neutral tank 9160 be moved to second via pump 9136 and hold tank.By continuing conventional cleanup acid treatment 9100 in batches by the dilute acid solutions in pickling container 9120 is emptying, and then to container 9120, fill water rinse solution.Pond pump 9150 is caught the overflow of water rinse solution, and this overflow is moved to neutral tank 9160 and/or holds tank.This processing 9100 can be by by emptying continuation of water rinse solution in container 9120, and then container 9120 filled to causticity purificants.Pond pump 9150 can be caught similarly overflowing of causticity rinsing solution and be moved to neutral tank 9160 and/or hold tank (not shown).

After material containing charcoal 9570 is by scale removal, it leaves this batch cleanup acid treatment 9100(via charcoal transferpump 9134) and enter conventional (as, Zha Dela wash-out) in batches wash-out and process 9200.As shown in Figure 29, conventional wash-out in batches processing 9200 generally includes from adsorption system 9700 de-sludging material containing charcoal 9500 and/or material containing charcoal is directly fed to elution containers 9240.The cylindrical tank that elution containers 9240 is normally large, its material be applicable to by reagent remain on rising pressure and temperature (as, 138 degrees Celsius-148 degrees Celsius) material.The material containing charcoal 9500 of this scale removal is maintained in elution containers 9240 under high temperature and pressure, and this container has the caustic-alkali aqueous elution solution of prussiate.After for some time, will give up charcoal 9550 from elution containers 9240 remove (as, via charcoal transferpump 9232), and moved to charcoal treatment system or charcoal regeneration system rapidly 9300 ' or processed 9300.Along with the material leaching being adsorbed to before on material containing charcoal enters elution solution, in elution containers 9240, form hot electrolyte solution 9421.Also from elution containers 9240, remove hot electrolyte solution 9421, and it is cooling for carrying out before entering conventional electrolytic deposition system 9400 ' in batches or processing 9400 by the heat exchanger that heats stand 9250 or be equal to.The cooling formation low-temperature electrolytes of hot electrolyte solution 9421 solution 9530 is necessary, to reduce the risk of the flash distillation in conventional electrolytic metal recovery unit 9420 in batches.Heating stand 9250 also as the colder lean solution 9540(by making to discharge from electrolytic metal recovery unit 9420 as, at approximately 66 degrees Celsius) warm and recovered energy, and/or before entering again elution containers 9240, make the lean solution of discharging lean solution hold-up vessel 9220 warm, to be used as again elution solution re-leaching reagent.Making cooling lean solution 9237,9540 warm to form hot lean solution 9239 also can use well heater to complete by using well heater or substitute heating stand 9250 except described heating stand 9250.Substantially use one or more pumps 9234,9236 so that lean solution is transmitted back to elution containers 9240.Can as required the additional agents from agent treated system and/or more mother liquor be added to lean solution tank 9220.

As shown in Figure 30, electrolyte solution 9530 enters the conventional ionogen metals recovery units 9420 in batches to work in batch circulation.The plate negative electrode of one group of parallel connection is arranged within the scope of close proximity, and electrolyte solution 9530 is pumped into and stir around this negative electrode.The body part of unit 9420 is loaded with the electric charge with cathode opposite, and by electrolysis, in electrolyte solution 9530, contained ion accumulates on negative electrode subsequently as the cathode slurry enriched material of recovery metal or as solid state cathode metal plating.At work, in batch processing step, conventionally negative electrode side by side 9420 is removed from unit, to collect the metal of this withdrawal.In the situation that using plate negative electrode, negative electrode can be flexible with from cathodic disbondment and remove hard cathodic metal coating.Using in other situation of higher deposition gauze (that is, " netted ") negative electrode, in processing subsequently by enriched material from cathodic disbonding, and then by cathode recirculation.Can be in unit 9420 bottom collect sludge enriched material, and can periodically remove.Electrolytic deposition pump box 9440 and pump 9430 are temporarily stored 9420 waste cell melts that remove (that is, lean solution) from unit between being used in batches.

The problem relevant with processing 9100 to above-mentioned conventional pickling system 9100 ' is a lot.For example, system is used independent, discontinuous " in batches " treatment step, and it needs constant manpower, stop time and energy (as, by the identical pickling container 9120 emptying rinse reagent different with filling continuously).In addition, this routine batch cleanup acid treatment 9100 is abandoning expensive acid, caustic alkali and/or other reagent conventionally after each use.This increased overhead (as, purchase cost, processing cost), and environment is caused to unnecessary harm.In addition, each conventional pickling container 9120 is drained to lay equal stress on fills different rinsing solutions, charcoal (with your mineral/metal attached to it) may not be recovered, this is due to heat, friction, the pump residence time and the exposure that extend, the pipe bend of increase and the quantity of valve, and the system that the useless rinsing solution that may still contain a small amount of material containing charcoal and precious metal frequently abandoning causes is inefficient.(not shown), if use separated container in each rinse step of acid cleaning process, needs nearly four tanks and ten pumps in other cases.This has increased original equipment overhead cost and integral device floor space.

Processing 9200 relevant problems to above-mentioned conventional wash-out in batches also has a lot.For example, process 9200 and use batch processing, its require constant manpower and energy (as, at every turn by wash-out container 9240 continuously emptying and heavily fill new elution solution, hot lean solution 9239 and material containing charcoal 9500 will need more electrolyte solution 9530 for electrolytic deposition 9400).This increased overhead cost (as, manpower, maintenance), make production process more complicated, and can endanger environment.In addition, and below the system 100 ' of the continuous extraction for metal of (Figure 22) according to the present invention of explanation is compared, conventional METAL EXTRACTION system 9000 ' is very heavy, and needs large equipment layout floor space as shown in figure 23.In addition, conventional elution system has limited operation velocity of flow, temperature and pressure, and it raises radiation loss and energy expenditure.In addition, the electrowinning of the metal of conventional " in batches " electrolytic deposition processing 9400 of above-mentioned use needs interrupt and a large amount of manual works the nonproductive fault-time of electrolytic deposition unit 9420, and it can cause too early cathode abrasion and useless electrolyte solution 9530.

Use zinc precipitates rare metal process from mother liquor or costliness is more inefficient for large operation, only effective to some metals, and can cause less rare metal recovery.

Summary of the invention

Therefore, the object of this invention is to provide improved metal recovery system, it is configured for continuous carbon and loads/absorption, continuous washing and the elution of material containing carbon, continuous ionogen forms, continuous electrolytic deposition, and continuous regeneration/reactivate, thus avoid recycling relevant the problems referred to above to conventional batches of metal.

Another object of the present invention be improve the efficiency that metal recovery processes (as, by minimizing radiation loss, reduce watt consumption, reduce reagent consumption, and anti-blocking decomposes and electrolyte losses).

Another object of the present invention is to prevent or minimize carbon loss and reagent waste.

Another object of the present invention is to maximize total metal recovery.

Another object of the present invention is to provide METAL EXTRACTION system, and it is configured to than conventional metal recovery system cost reduction and has less floor space.

Another object of the present invention is to provide the system and method for metal recovery, and it is configured to than the higher velocity of flow of ordinary method, temperature and/or pressure work.

Still another object of the present invention is the not recovery weight metal per-cent reducing in useless ionogen/lean solution.

According to accompanying drawing and explanation here, these and other objects of the present invention will be clearly.Although each object of the present invention is believed by least one embodiment of the present invention, realize, yet any one embodiment of the present invention there is no need to realize all objects of the present invention.

System for the continuous recovery of metal is provided.According to certain embodiments of the present invention, this system comprises at least one in continuous pickling system, continuous elution system, continuous electrolysis depositing system, continuous pickling system is configured to receive inflow continuous, unbroken material containing carbonaceous particle, and carries outflow continuous, unbroken de-sludging material containing carbonaceous particle; Elution system is configured to receive inflow continuous, unbroken elution solution that contains de-sludging material containing carbonaceous particle continuously, and carries outflow continuous, unbroken electrolyte solution; And continuous electrolysis depositing system is configured to receive inflow continuous, unbroken electrolyte solution, carry and not to interrupt continuously the outflow of lean solution, and continuously and interruptedly do not form negative electrode sludge enriched material.Continuous pickling system, each of continuous elution system and continuous electrolysis depositing system is substantially configured to work simultaneously and there is no total periodic interrupt in conventional batches of metal recycling.

In some embodiments, this system can comprise the integrated carbon regeneration system rapidly that may be operably coupled to continuous elution system.Continuous carbon loading/absorption system can may be operably coupled to the upstream of continuous pickling system.Continuous pickling system can may be operably coupled to continuous elution system; For example,, by the tank that holds between described continuous pickling system and described continuous elution system.Can provide one or more pumps for promoting the conveying of slurry and solid and system.In a preferred embodiment, elution system may be operably coupled to continuous electrolysis depositing system and comprises one or more filter screens or strainer continuously, and it is configured to prevent that carbonaceous particle from arriving continuous electrolysis depositing system.

This continuous pickling system can comprise chamber, and it is configured to keep fluidizing medium; Entrance, it is configured for and receives the charging that contains material containing carbonaceous particle; Fluidized-bed distribution plate or other devices, it is configured to fluidisation material containing carbonaceous particle in the situation that described fluidizing medium exists; Opening, it is configured to material containing carbonaceous particle and fluidizing medium to carry from chamber; And screen cloth, it is configured to filter material containing carbonaceous particle from fluidizing medium.This continuous elution system can comprise ejecting container, continuous wash-out container, and flash chamber, wherein ejecting container can operationally be connected in series to continuous wash-out container, this continuous wash-out container can operationally be connected in series to flash chamber, and this ejecting container can operationally be connected in parallel to flash chamber.This continuous electrolysis depositing system comprises electrolysis cells, and it has the unit body that is configured to electrolyte solution to remain on high pressure and/or temperature; At least one anode; At least one negative electrode; Entrance, it is configured to receive inflow stream continuous, unbroken electrolyte solution; The first outlet, what it was configured to discharge waste cell melt solution continuously, does not interrupt flowing out stream; The second outlet, is configured to remove negative electrode sludge enriched material; And dwell chamber, it is configured to electrolyte solution to be delivered to continuously described the first outlet from described entrance, and extends the residence time of described electrolyte solution between described at least one anode and described at least one negative electrode.This dwell chamber can comprise one or more passages, it is configured to provide therein pressurization streams of electrolyte solution, it is enough by force to evict from continuously along described one or more passages and/or to carry negative electrode sludge enriched material, and finally from described dwell chamber, discharges.

This continuous wash-out container can comprise the inflow manifold being communicated with the first outlet and the entrance of electrolysis cells respectively and flow out manifold, and also comprise fluidized-bed and/or one or more Internal baffle, it is configured to crooked flowing-path and extends the material containing carbonaceous particle residence time therein.Valve is also provided, and it is configured to the solution that flash distillation (flash) is left continuous wash-out container and entered flash distillation (flash) container.

This continuous pickling system can comprise at least one in acid solution, the aqueous solution and alkaline solution.This continuous elution system can comprise the solution containing with lower at least one: material containing has the carbonaceous particle of precious metal, electrolyte solution, useless carbonaceous particle, caustic alkali, water composition and prussiate.This continuous electrolysis depositing system can comprise electrolyte solution or negative electrode sludge enriched material.Continuous pickling system, each in elution system and continuous electrolysis depositing system can be configured to the solution that wherein held or slurry to extend the residence time continuously, increases pressure, or rising temperature, and can comprise screen cloth or filter element.

In some embodiments, this continuous pickling system can comprise a plurality of washing containers, and each washing container comprises the chamber that is applicable to hold fluidizing medium; For receiving the entrance of the charging that contains material containing carbonaceous particle; Be used for by fluidized-bed distribution plate or other device of described fluidizing medium fluidisation and clean material containing carbonaceous particle; Opening, it is configured to carry material containing carbonaceous particle and fluidizing medium from described chamber; And screen cloth, it is configured to filter material containing carbonaceous particle from fluidizing medium.For example, in some embodiments, this continuous pickling system can comprise the pickling tank that accommodates acid fluidizing medium, accommodates the water rinse tank of basic pH-neutral aqueous solution, and the alkali rinse tank that holds alkaline fluidizing medium.

In some embodiments, this continuous pickling system can comprise for collecting one or more recirculation tanks of useless fluidizing medium, and for collecting one or more overflow weirs of useless fluidizing medium, passage, valve, or water shoot.This continuous electrolysis depositing system can be configured to continuously and interruptedly not collect and remove described negative electrode sludge enriched material, and can comprise the one or more passages that are limited between negative electrode, anode and isolator.These one or more passages can comprise volution, scroll, and pitch of the laps, compound curve, 3D-SPL, 8-shaped, or sinuous part, and negative electrode and anode can form sleeve or the pipe of being separated by described isolator.In some embodiments, carbon regeneration system rapidly can may be operably coupled to continuous elution system and continuous carbon loading/adsorption system, and described continuous carbon loading/adsorption system may be operably coupled to described continuous pickling system.

A kind of method of the continuous recovery for metal is disclosed.According to some embodiments, the method comprise to continuous washing system continuously feeding be loaded with the particle of metal; In described continuous washing system, wash continuously described material containing particle with by the de-sludging of described material containing particle; From described continuous washing system, remove continuously de-sludging material containing particle; To continuous elution system, load continuously described de-sludging material containing particle; From described continuous elution system, remove continuously electrolyte solution; To continuous electrolysis depositing system electrolyte solution described in feeding continuously; From described continuous electrolysis depositing system, remove continuously waste cell melt solution; Described waste cell melt solution is delivered to described continuous elution system continuously; Wherein said continuous washing system, described continuous elution system, and each in described continuous electrolysis depositing system is operably connected and is configured to allow above-mentioned steps to carry out simultaneously, and there is no periodic interrupt required in conventional batch processing.

The method also can comprise from continuous elution system and remove continuously useless particle; Described useless particle is fed to carbon regeneration system rapidly continuously; From continuous electrolysis depositing system, remove continuously negative electrode sludge enriched material; And/or by metal being adsorbed on continuously and forming described material containing particle on described particle with described continuous washing system similarity or identical continuous carbon loading/adsorption system.Described particle can be a kind of in carbonaceous particle, polymer absorbant or ion exchange resin.

Accompanying drawing explanation

Fig. 1 and 2 schematically shows the system and method for the continuous recovery of metal according to some embodiments;

Fig. 3 is according to the schema of three of some embodiments continuous pickling operation in succession;

Figure 4 and 5 show the step of processing according to the continuous pickling of some embodiments;

Fig. 6 and 7 shows the washing tank that can be used for the cleanup acid treatment shown in Fig. 1-5;

Fig. 8 shows the pickling system that comprises a plurality of washing tanks shown in Fig. 6 and 7;

Fig. 9 and 12 schematically shows according to the system and method for the continuous wash-out of some embodiments;

Figure 10 surveys view according to the axle that waits of the continuous elution system of some embodiments;

Figure 11 shows the sectional view of the continuous elution system of Figure 10;

The system and method for Figure 13 and the 19 schematically illustrated depositions of the continuous electrolysis according to some embodiments;

Figure 14 shows according to the top view of the continuous electrolysis depositing system of some embodiments;

Figure 15 and 16 be respectively along the continuous electrolysis depositing system of the line XV-XV intercepting of Figure 14 vertically and etc. isometric cutaway view;

Figure 17 is the detailed view of Figure 15, shows according to the details of the entrance of some embodiments;

Figure 18 is the sectional elevation along the electrolytic deposition unit of the line XVIII-XVIII intercepting of Figure 14;

Figure 20 is the processing for the useless charcoal of regenerate/reactivate according to some embodiments;

Figure 21 and 22 shows the system for the continuous recovery of metal;

Figure 23 shows the conventional batch system for the recovery of metal;

Figure 24 shows the washing tank shown in Fig. 6-8 or for the alternate embodiment of the device of load/absorption of continuous carbon;

Figure 25 shows the concrete axle that waits of the chamber shown in Figure 24 and surveys view;

Figure 26 shows the sectional view of chamber shown in Figure 25;

Figure 27 shows the conventional system for the recovery of metal;

Figure 28 shows conventional cleanup acid treatment;

Figure 29 shows conventional wash-out in batches and processes; With

Figure 30 shows conventional electrolytic deposition in batches and processes.

Embodiment

As shown in figs. 1 and 2, according to certain embodiments of the present invention, for continue device systems 100 ' or the method 100 of recovery (recovery) metal from mineral (mined ore), comprise, continuous pickling (acid wash) system 10 ' or method 10, continuous wash-out (elution) system 20 ' or method 20, continuous electrolytic deposition (electrowinning) system 40 ' or method 40, continuous charcoal regeneration (continuous carbon regeneration) system 30 ' and method 30, and load/absorption of continuous charcoal (continuous carbon loading/adsorption) system 70 ' or method 70.It can for example obtain activity/regenerated carbon 56(from cocoa shell or charcoal), or alternatively, the particulate matter that is equal to such as the polymer absorbant (adsorbent) of material containing (loaded) or the ion exchange resin of material containing etc. experiences continuous charcoal adsorption treatment 70, in this processing, it is spent in mother liquor (pregnant solution) and stops the time suspending, the target that this mother liquor contains dissolving is extracted metal, as gold and silver, aluminium, platinum, uranium, chromium, zinc, cobalt, manganese or lead.Charcoal loading/adsorption system 70 ' or method 70 that this is continuous can comprise, for example, as Fig. 6 and 7 or Figure 24-26 as shown in device, it is for by the activity/regenerated carbon of mother liquor 56 fluidisations (fluidize).Once charcoal 56 has been loaded target and has extracted metal, it experiences continuous cleanup acid treatment 10.Scale removal (descaled) the material containing charcoal 50 that leaves continuous pickling processing 10 enters and holds tank 60, its be equipped with comprise one or more reagent (reagent) (as, water, etching reagent and prussiate) elution solution (strip solution) to form the slurry 51 of elution solution and scale removal material containing charcoal 50.This slurry 51 enters continuous wash-out and processes (elution process) 20, wherein the temperature of slurry 51 and/or pressure increase and the target of being adsorbed by charcoal before extract metal by re-leaching (releach) to elution solution, thereby form, can be used for continuous electrolytic deposition and process 40 electrolyte solution 53.From continuous electrolytic deposition, processing 40 lean solutions of leaving (that is, waste electrolyte) 54 is back to continuous wash-out processing 20 and/or holds tank 60 to reuse.The solid fragment 55 that emptying its target is extracted the waste active carbon of metal via continuous elution process 20 moves to charcoal manipulation of regeneration 30, to be used further to carrying out reactivate before continuous charcoal loading/adsorption process 70.

As shown in Fig. 2-5, continuous cleanup acid treatment 10 can roughly comprise the following steps: by 57 feedings 1004 of material containing charcoal to continuous pickling system 10 ', in the first pickling tank 12, will in dilute acid solutions, enter material containing charcoal 57 fluidisations 1006, from pickling tank 12, extract 1008 material containing charcoals, the material containing charcoal that screening (screening) 1010 extracts is to remove dilute acid solutions, collect the 1012 dilute acid solutions 57c from the separation of material containing charcoal, the dilute acid solutions 57c(that processes alternatively 1014 these collections as, filter, additive, pH regulator), and by being back to pickling tank (tank) 12, dilute acid solutions 57c feeding reclaims this dilute acid solutions 57c.The acid of the acid bath (acid bath) through in pickling tank 12 is floated to (acid-rinsed) material containing charcoal 57a feeding 1018 to the second water that holds water or another kind of pH-neutral water and float (aqueous rinse) solution 57d and float tank 14, and then at described water, float in tank 14 and be fluidized 1020.Process 10 and also comprise that from water, floating tank 14 extracts 1022 rinsing material containing charcoal 57b, the rinsing material containing charcoal 57b of screening 1024 these extractions floats solution 57d to remove water, collect 1026 and float solution 57d from the Separation of Water of rinsing material containing charcoal 57b separation, the water of processing alternatively 1028 these collections float solution 57d(as, filtration, additive, pH regulator), and by water being floated to solution 57d feeding 1030 is back to that water floats tank 14 and recycle-water floats solution 57d.The rinsing material containing charcoal 57b that floats in tank 14 experience washing at water is fed 1032 and floats tank 16 to the 3rd alkali that accommodates alkali and float (caustic rinse) solution 57e, and then at this alkali, floats in tank 16 and be fluidized 1034.This continuous pickling is processed 10 and is also comprised that from alkali, floating tank 16 extracts 1036 scale removal material containing charcoals 50, the scale removal material containing charcoal 50 of screening 1038 these extractions floats solution 57e to remove alkali, collect 1040 and float solution 57e from the alkali of scale removal material containing charcoal 50 separation, process alternatively 1042 collected alkali float solution 57e(as, by filtering, provide additive or regulating pH), and float tank 16 and reclaim alkali and float solution 57e by solution 57e feeding 1044 being back to alkali.Continuous cleanup acid treatment 10 can comprise provides one or more pump 13a, 13b for by the step of rinsing solution tank 12,14,16 recirculation described in each.Alternatively, can provide the 4th water to float circulation (not shown), and it will be understood by those skilled in the art that any one or more above-mentioned water-washing steps can repeat or substitute.

Refer now to Fig. 6 and 7, for material containing particulate material being cleaned to any part that can be used for continuous pickling processing 10 with the pickling tank 200 of de-sludging.The material containing particulate material of washing in described pickling tank 200 can be any particle size, shape and density, and it can carry out fluidisation or be suspended in cleaning in fluidizing medium by cleaning fluidizing medium.Pickling tank 200 is advantageously configured to will be loaded with the activated carbon granule scale removal of metal target, for preparing to form electrolytic deposition electrolytic solution used.In this case, pickling tank 200 can be filled with and comprise sour fluidizing medium.Similar tank 200 ', 200 " can use the fluidizing medium that comprises water or caustic soda.In addition, similar tank can be used for other other processing, continuous charcoal loading/adsorption treatment 70 for example, wherein particle comprises activity/regenerated carbon 56, and fluidizing medium comprises mother liquor, it forms by permeating prussiate and/or other reagent heap leaching pad (heap leach pad) by the ore that contains metal target or mineral of fragmentation.

According to some embodiments, pickling tank 200 can comprise pickling tank, it has the first chamber 220, first fluidized bed distribution plate 221, the first entrance 222, the first recirculation entrance 223a, the first recirculation outlet 223b, the first overflow weir (weir) 224, the first screen cloth 226, outlet 228, the first recirculation tanks 229 are discharged in the first overflow outlet 227, the first, diapire 260, inner tubal wall 266, outer tube wall 268, and be limited to the first channel 282 between inner tubal wall 266 and the outer tube wall 268 adjacent with the first overflow weir 224.The first screen cloth 226 for by by liquid portion (as, waste liquor, fluidizing medium, or conveyance fluid) separated and filter and enter feeding from solid particulate part (metal loads material containing or heavy duty material charcoal).The liquid portion of discharging from particle is maintained at the first recirculation tank 229, and can remove via the first recirculation outlet 223b.The first recirculation outlet 223b can be sealed in operating process, is connected to and holds tank, is connected to water shoot, is connected to water pump, or is additionally configured to feeding upstream or downstream processing.

In some embodiments, as shown in Figure 8, continuous pickling system 10 ' can comprise the one or more independent cleaning of evaporator 200,200 ', 200 being connected in series ", to arrange and/or to reduce to provide handiness in whole floor space at equipment for customizing.In some cases, tank 200,200 ', 200 " can comprise similar or identical DESIGNED FEATURE, comprise respectively different fluidizing mediums.For example, in some embodiments, the first tank 200 can comprise pickling tank, and it accommodates dense or dilute acid solutions 57c, thereby the 2 200 ' and the 3 200 " tank can comprise water and alkali rinse tank, it accommodates respectively water 57d and alkali 57e purificant.Although do not require, however tank 200,200 ' and 200 " can be constructed to " general " or " interchangeable " tank.In addition, tank 200,200 ' and 200 " can be configured the pipe shown in having (as, cylindrical tube or prism are extruded (prismatic extrusion)) shape, to reduce manufacturing expense.Any one or more tanks 200,200 ' and 200 " replaceable be the tank of different size, or the tank as shown in Figure 24-26 2000, it will be described below.

The first class medium that comprises dilute acid or scale inhibitor solution can occupy the first pickling tank 200.In some embodiments, first class medium can comprise the solution of 1-10% volume/volume (vol/vol) mineral acid, for example, be configured to dissolve nitric acid or the hydrochloric acid of charcoal silicate dirt.In use, enter the first chamber 220 that the material containing charcoal 57 of material containing/again moves through the first screen cloth 226 via the first entrance 222 and flows into the first pickling tank 200.Have that the material containing of entering/fluid of material containing charcoal 57 is discharged from and enters the first recirculation tank 229 again.The material containing charcoal of screening one after the other falls downwards and towards first fluidized bed distribution plate 221 along the first screen cloth 226, and by first class medium fluidisation.First class medium enters the first recirculation entrance 223a and passes through distribution plate 221.The first class medium of clarification rises to the higher suspension level top of material containing charcoal in the first pickling tank 200, and fills with on the first overflow weir 224 and entered first channel 282.After this, the first class medium of clarification is discharged from the first pickling tank 200 via outlet 227, and is fed into alternatively the first recirculation entrance 223a and first fluidized bed distribution plate 221.One or more pump 13a can be arranged between outlet 227 and entrance 223a.

Acid is floated the slurry of material containing charcoal 57a and residue first class medium and is discharged from the first pickling tank 200 via the first outlet opening 228, and via the second entrance 232, enters the second water and float tank 200 '.This acid is floated material containing charcoal 57a and can only be used gravity to be transported to tank 200 ', or this acid is floated material containing charcoal 57a and can be used one or more mashing pump (not shown) to be transported to tank 200 '.Such as the second fluidizing medium of pH-neutral water washing soln or hot water roughly, can occupy the second water rinse tank 200 '.In use, acid rinse material containing charcoal 57a and first class medium move through the second screen cloth 236 or are equal to strainer, and then flow into the second chamber 230 for preimpregnation.The second screen cloth 236 is separated for residue first class medium liquid is floated to material containing charcoal 57a from acid, and the first class medium of wherein discharging is maintained in the second recirculation tank 239, and can be removed via the second recirculation outlet.This second recirculation outlet 233b can be connected to and hold tank, filtration unit, or upstream or downstream processing.For example, as the dashed path of dilute acid solutions 57c ' is schematically indicated, the second recirculation outlet 233b can may be operably coupled to the first recirculation entrance 223a, with by material containing charcoal 57 fluidisations of the material containing in the first rinse tank 200/again.Although not shown, can one or more pumps are arranged between outlet 233b and entrance 223a.

After passing through the second screen cloth 236, acid is floated material containing charcoal 57a subsequently towards the second fluidized-bed distribution plate 231 whereabouts, and by entering the second recirculation entrance 233a and being upwards fluidized in the second chamber 230 by the flowing of the second fluidizing medium of plate 231.The second fluidizing medium that does not contain the clarification of material containing charcoal particle rises to the suspension level top of pickling material containing charcoal, and filled with on the second overflow weir 234 and entered second passage 284, wherein it floats that tank 200 ' is discharged and feeding the second recirculation entrance 233a and the second fluidized-bed distribution plate 231 alternatively via outlet 237 from the second water, and the dashed path institute of floating solution 57d as water is schematically illustrated.

The slurry of rinsing material containing charcoal 57b and the second fluidizing medium is discharged from the second rinse tank 200 ' via the second outlet opening 238, and enters the 3rd rinse tank 200 via the 3rd entrance 242 ".Rinsing material containing charcoal 57b can only be used gravity to be transported to the 3rd alkali to float tank 200 ", or rinsing material containing charcoal 57b can be used one or more pump (not shown) to be transported to tank 200 ".The 3rd fluidizing medium that floats solution such as alkali can occupy the 3rd rinse tank 200 ".For example, the 3rd fluidizing medium can comprise a certain amount of sodium hydroxide (NaOH) or 0.5% and 5%wt between, 1%wt for example, potassium hydroxide (KON).The 3rd fluidizing medium can comprise other reagent, as the sodium cyanide of 1-10%wt (NaCN).The 3rd fluidizing medium can be heated (as, 20-100 degree Celsius).In use, the strainer that the slurry of rinsing material containing charcoal 57b and the second fluidizing medium flows through the 3rd screen cloth 246 or is equal to, and enter the 3rd chamber 240.The 3rd screen cloth 246 for by by the second fluidisation medium liquid part from separated this slurry that filters of its rinsing material containing charcoal 57b solid part.The second fluidizing medium of this separation is maintained in the 3rd recirculation tank 249.The second fluidizing medium can remove from tank 249 via the 3rd recirculation outlet 243b, and the 3rd recirculation outlet 243b can be connected to and hold tank, filtration unit, or one or more upstream or downstream processing.For example, as schematically indicated in the path of water rinse solution 57d ', the 3rd recirculation outlet 243b can may be operably coupled to the second recirculation entrance 233a, helping the particle in fluidisation the second water washing tank 200 '.Although not shown, can one or more pumps are arranged between outlet 243b and entrance 233a.In some cases, outlet 243b and entrance 233a can may be operably coupled to equipment water system.

After through the 3rd screen cloth 246, the material containing charcoal particle of twice rinsing falls subsequently to the 3rd fluidized-bed distribution plate 241, and by entering the 3rd recirculation entrance 243a and being fluidized in the 3rd chamber 240 by the flowing of the 3rd fluidizing medium of plate 241.The 3rd fluidizing medium of clarification is increased to tank 200 " in the higher suspension level top of material containing charcoal of fluidisation; and filled with the 3rd overflow weir 244 and entered third channel 286; wherein it floated tank 200 via outlet 247 from alkali " discharge, and alternatively as alkali float the dashed path of solution 57e indicated be fed into the 3rd recirculation entrance 243a.

Alkali floats, the slurry of de-sludging material containing charcoal 50 and the 3rd fluidizing medium via the 3rd outlet opening 248 from the 3rd alkali rinse tank 200 " discharge, and can be sized subsequently or filter for further processing.Leaving tank 200 " afterwards; the de-sludging material containing charcoal 50 in slurry can be separated from the 3rd fluidizing medium liquid portion by screen cloth or strainer (not shown); and then add in the elution solution of the water, alkali and the prussiate that hold in tank 60, for the continuous wash-out 20 in downstream and electrolytic deposition 40, process.

In use, shown in, reduce or eliminate continuing to buy and change the needs of the loss amount of charcoal particle, water, alkali, acid and/or antiscale reagent with described continuous pickling system 10 '.System 10 ' has also reduced significantly needs the amount of lean solution to be processed and charcoal, and has reduced the potential hazard to environment.

Should be appreciated that, it is in fact schematically and not should limit the scope of the invention that the specific features of continuous pickling system 10 ' described herein and suggestion are used.For example, Fluidized Bed Partial 221,231,241 can be replaced by or in conjunction with one or more machinery or pressure air agitator (not shown) with the material containing charcoal particle that suspends in fluidizing medium.In addition more or less shown in comparable of the quantity of the chamber 220,230,240 of each system 10 '.In some embodiments, relative size, size and/or the variable volume of chamber 220,230,240.In other embodiments, chamber 220,230,240 can be set to similar size and ratio.In addition, can be by one or more tanks 200,200 ', 200 " setting parallel to each other, to increase turnout.For example, the 3rd alkali rinse tank 200 of system 10 ' " can be connected to directly or indirectly a plurality of upper water rinse tanks 200 '.Can be by separating (splitting) entrance 222,223a; 232,233a; 242,243a and/or outlet 223b, 227; 233b, 237; 243b, 247, any one the single tank 200 in the replaceable system 10 ' of a plurality of tanks 200.In addition, any one chamber 220,230,240 can be spaced as a plurality of chambers.As mentioned before, system 10 ' or its part are used in and in continuous carbon loading/adsorption process 70, are written into continuously gac.For example, feeding particle can comprise activity and regenerated carbon, and first, second, and third fluidizing medium can comprise mother liquor (as, contain sodium cyanide (NaCN) solution that dissolves precious metal).

Fig. 9 shows according to the continuous wash-out of some embodiments and processes 20.The feeding slurry 51 of elution solution and scale removal material containing charcoal 51 is moved into ejecting container (splash vessel) 22 by gravity or one or more pump 23.These ejecting container 22 increases enter temperature and/or the pressure of slurry 51, and the grouting material 51 that adds of heat is delivered to continuous wash-out container 24.In this continuous wash-out container 24, be adsorbed to before metal target on material containing charcoal leached (leach) to elution solution to form electrolyte solution 53.This electrolyte solution 53 filters via one or more screen clothes, with move to continuous electrolytic deposition will give up before processing 40 charcoal and not elution material containing charcoal from electrolyte solution 53, remove.Electrolyte solution 53 can be transported to continuous electrolytic deposition processing via discharge manifold (effluent manifold) 28b being arranged on continuous wash-out container 24.The waste slurry 51c of elution solution and useless charcoal is flashed and enters flash chamber (flash vessel) 25 by valve 27, wherein steam is collected and is back to via steam-return line 21 ejecting container 22, to help heating and pressurized jet container 22 by efficient manner.By draining screen 26, resulting concentrated waste slurry 51d is separated into solid 55 and liquid 52 parts.The liquid portion 52 of thickened waste slurry 51d can be returned to and hold tank 60, and the solid part 55(of thickened waste slurry 51d is, useless dehydration charcoal) can be sent to charcoal manipulation of regeneration 30 for regeneration.The lean solution 54 of returning from continuous electrolysis depositing treatment 40 roughly utilizes immersion heater 27 to be heated, and then via one or more pumps 23 and inflow manifold 28a, is back to continuous wash-out container 24.

Figure 10 shows the continuous elution system 20 ' according to some embodiments.This continuous elution system 20 ' comprises the continuous wash-out container 24 of the first ejecting container 22, the second being connected in series by pipeline section substantially, and the 3rd flash chamber 25, and splash 22 and flash distillation 25 containers between the steam-return line 21 that extends abreast.One or more pumps 23 can be arranged on the different piece of system 20 ', to promote the flow direction, stream from container 22,24,25, the other parts of system 20 ', and/or the other parts in system 100 ' 10 ', 30 ', 40 ', and circulate between it, for extracting continuously metal.

As shown in Figure 11, continuous wash-out container 24 comprises fluidized-bed distribution plate 320, and it by dwell chamber (residence chamber) 340 from fluidisation chamber 350 separately.Can various configurations (as, quantity, angle, interval, geometrical shape) one or more baffle plates 318 are arranged in dwell chamber 340, to increase, enter heat and add the residence time of grouting material 51a in wash-out container 24 continuously.These one or more baffle plates 318 can the parallel and staggered sinuous flowing-path 51b that adds grouting material 51a to form heat.This baffle plate 318 can be parallel, not parallel, staggered at single predetermined angular, or arrange in an alternating manner from each baffle plate that is orientated different predetermined angulars.Should understand and can use other baffle shapes and layout and not restriction, and the shape of baffle plate 318, porosity and/or quality can from shown in different.For example, any one or more of baffle plate 318 can comprise folding, turning, bending, ripple, opening, trellis etc.

Pulp flow in wash-out container 24 can comprise that entering heat adds grouting material 51a and leave continuous electrolysis depositing system 40 ' or process 40 lean solution 54 continuously.Can via one or more influxs 326 with influx frame 322, be fed to fluidisation chamber 350 by being connected to the inflow manifold 28a of continuous wash-out container 24.Alternatively, flow into one or more sidewalls 310 that manifold 28a can alternatively be connected directly to continuous wash-out container 24.One lean solution 54 flows into continuous wash-out container 24 via flowing into manifold 28a.This fluid enters and fills fluidisation chamber 350, and the fluidized-bed 320 of flowing through is to help fluidisation and to help charcoal in dwell chamber 340 grain fluidized and suspend at it when the flowing-path 51b that wriggles moves.

Also for continuous wash-out container 24 arranges, discharge manifold 28b, to extract electrolyte solution 53 from dwell chamber 340, and this electrolyte solution 53 is delivered to continuous electrolytic deposition system 40 ' or processes 40.Discharge manifold 28b and comprise one or more discharge manifold ports, it can be provided with discharges manifold ports frame for being conveniently connected to continuous wash-out container 24.Manifold 28a is similar to flowing into, and discharges manifold 28b and can be connected directly to one or more sidewalls 310 of continuous wash-out container 24, or can be connected to container 24 via having one or more relief outlets 316 of relief outlet frame 312.

In the time of in the dwell chamber 340 of continuous wash-out container 24, material containing charcoal is exposed to elution solution reagent under high temperature and high pressure condition.Reagent in this elution solution is for metal content from material containing charcoal elution absorption before it (as, gold), and it " is leached " to solution to form electrolyte solution again.One or more screen clothes or strainer 324 can be arranged on dwell chamber 340 and discharge between manifold 28b and extract electrolyte solution 53 streams of clarification and/or prevent that charcoal particle from flowing to the downstream of discharging manifold 28b with the wash-out container 24 from continuous.In some embodiments, as shown in the figure, the position of described screen cloth or strainer 324 can be in the relief outlet of continuous wash-out container 24 and the interface between one or more sidewall 310.Yet, screen cloth or strainer 324 can be arranged on to other position and not restriction, for example: in discharging manifold 28b, in continuous wash-out container 24, in the interface of discharging between manifold 28b and frame 312, or in the downstream of discharging manifold 28b.Should be understood that and one or more sealing members or packing ring (not shown) can be arranged between inflow 28a or discharge 28b manifold and continuous wash-out container 24.

Fluidized carbon in dwell chamber 340 and solution continue to move along sinuous flowing-path 51b, until it is discharged to be used as ionogen via discharging manifold 28b, or by outlet 328.Outlet 328 can comprise export frame 330 and/or exit seal part 329, for being connected to valve 29.Valve 29 can be any kind known in the art, for example ball valve or miter valve and not restriction, and should understand valve and can be connected to individually one or two in continuous wash-out container 24 and flash chamber 25, or with continuous wash-out container 24 and flash chamber 25 in one or two integrally form.In addition, if the distance between continuous wash-out container 24 and flash chamber 25 is large, extra pipeline section can be added between the second opening 328 and valve 29.

The hot pressurization waste slurry 51c leaving from continuous wash-out container 24 is when by valve 29 " flash distillation ".The mixture of resulting gas vapor, fluid and solid enters overdraft flash chamber 25, and wherein heating steam is divided and flows back into ejecting container 22 via steam-return line pipe 21.Do not evaporate lean solution and useless charcoal and in the fluid of thickened waste slurry 51d, leave flash chamber 25.Thickened waste slurry 51d can comprise lean solution liquid portion 52 and solid part 55, and this solid part 55 is the precious metal that adsorbs before the substantially not have useless charcoal of (as, gold).As mentioned above, thickened waste slurry 51d fluid can be filtered or be sieved by draining screen 26 subsequently.

In the embodiment shown, by dehydration screen cloth 26, the liquid portion 52 of thickened waste slurry 51d is separated and be back to and hold tank 60 and make elution solution for re-using from solid part 55.One or more pump (not shown) can be arranged to liquid portion 52 to move to and hold tank 60.The solid part 55 of the useless charcoal of dehydration is sent to and comprises regeneratory furnace 35 or for the charcoal manipulation of regeneration 30 of other device of reactivate charcoal.Dehydration screen cloth 26 can be set to two-stage screen cloth, and wherein the first step is removed most of liquid portion 52 from useless charcoal solid part 55, and second stage solid part 55 from useless charcoal before it enters regeneratory furnace 35 or washing container is removed residue caustic alkali and/or prussiate.Therefore, there is no to damage the device in charcoal regeneration system rapidly 30 '.

The schematically illustrated continuous wash-out according to some embodiments of Figure 12 processes 20.The first, produce 1048 de-sludging material containing charcoals 50 and the slurry 51 that comprises the causticity elution solution of water and prussiate.Slurry 51 can form and be stored in and hold in tank 60.Then slurry 51 pumpings 1050 are entered to ejecting container 22, it is configured to promote temperature and/or the pressure of scale removal material containing charcoal/elution solution slurry 51.After the temperature and/or pressure 1052 of the slurry 51 in increasing ejecting container 22, the hot grouting material 51a that adds of material containing charcoal/elution solution forms and moves 1054 to continuous wash-out container 24 from ejecting container 22.The grouting material 51a that adds of this heat is maintained in container 24, be used for extending the residence time 1056, for example, by provide separately fluidized-bed 320 or with a plurality of plate washer 318 combinations, with extend heat add grouting material 51a at the entrance 304 of container 24 and export the physics mobile route between 328.For example, physics mobile route can be as directed sinuous flowing-path 51b.

In the time course stopping in continuous wash-out container 24, its precious metal adsorbing of material containing charcoal elution grouting material 51a that adds by the reagent in causticity (caustic) elution solution from heat.Therefore causticity elution solution is dissolved to itself by rare metal, thereby forms electrolyte solution 53.Electrolyte solution 53 is sieved to remove charcoal particle from it, and extract 1064 from continuous wash-out container 24.Subsequently, electrolyte solution 53 be fed 1066 to continuous electrolysis depositing system 40 ' (as, enter continuous electrolysis METAL EXTRACTION unit 42) for rare metal recovery (recovery).At electrolytic deposition, process (referring to Figure 19) in 1068 processes, lean solution 54 is removed 1070 from continuous electrolysis depositing system 40 ' constantly, and directly or indirectly (as, by lean solution, hold tank (not shown) or immersion heater) pumping 1072 is back to continuous wash-out container 24.

From continuous wash-out container 24, remove constantly solution and charcoal, and the liquid portion of solution before entering flash chamber 25 by valve 29 " flash distillation " or evaporate at least in part 1058.This processing 20 also comprises from the rapid evaporation of existing waste slurry 51c extracts 1060 heating steams, and vapour pipe is sent (piping) 1062 be back to ejecting container 22 effectively to increase temperature and/or the pressure of 1,052 first containers 22.Thickened waste slurry 51d is removed to 1074 from ejecting container 25, and then dewater 1076 with by waste liq part 52 from useless solid part 55 separation.This solid part 55 comprises dehydration charcoal, and it is sent 1078 to charcoal regeneration system rapidly 30 ', and the waste liq part 52 of thickened waste slurry 51d is sent 1080 to holding tank 60 to reuse.

Shown in should understanding here and the continuous elution system 20 ' of explanation and process 20 specific features and suggestion is used and is in fact exemplary and should not limits the scope of the invention.For example, fluidized-bed 320 is replaceable be or in conjunction with one or more mechanical stirrer (not shown) so that material containing charcoal particle suspend.In addition, continuous more or less shown in comparable of the quantity of the baffle plate 318 in wash-out container 24, to be provided for concrete the process required residence time and velocity of flow.In addition, one or more extra containers 22,24,25 can be added to continuous elution system 20 ', and arrange with productivity gain in series or in parallel with other container 22,24,25.For example, two or three continuous wash-out containers 24 can directly or indirectly be connected to each other in parallel, and are in series arranged between single ejecting container 22 and single flash chamber 25.

Figure 13 shows according to the continuous electrolytic deposition of some embodiments and processes 40.This processing 40 comprises provides ionogen to hold liquid 53 continuously, feeding electrolyte solution 53 is to continuous electrolysis matter METAL EXTRACTION unit 42 continuously, in unit 42, from sludge thing, remove stream (sludge removal stream) 53g and extract negative electrode sludge enriched material 53f, from unit 42, extract continuously lean solution 54 and carry out the continuous wash-out container 24 the continuous elution process 20 of feeding by this lean solution 54.

As shown in Figure 14-18, continuous electrolysis depositing system 40 ' comprises continuous electrolysis matter METAL EXTRACTION unit 42 substantially, it comprises cell body 406, this cell body 406 has first end 440, the second end 480, the one or more sidewalls 482 that extend betwixt, there is the base 404 of one or more 402, at least one entrance 410 becoming a mandarin for receiving the Continuous Flow of the electrolyte solution 53 that contains precious metal, at least one first outlet 420 of the continuous outlet of the lean solution 54 that is used for providing useless fluid electrolyte 53d and wherein contains, and at least one second outlet 430 of the outlet of the negative electrode sludge enriched material 53f that unit 42 collects is provided.This second outlet 430 can be configured for the continuous discharge of the negative electrode sludge enriched material 53f of collection, or the second outlet 430 can be configured to the discharge at intermittence of the negative electrode sludge enriched material 53f of described collection.In cell body 406, be provided with the first chamber 405, the second chamber 407, the 3rd chamber 408 and dwell chamber 460, dwell chamber 460 comprises one or more elongate channel 462.This passage 462 is configured to increase the residence time of electrolyte solution 53, and the forced-flow of the electrolyte flow 53b of electrolyte solution 53 is provided therein, and this flows enough strong so that the negative electrode sludge enriched material that forms and accumulate in passage 462 is evicted from and/or to be removed.These one or more passages 462 can comprise for example spiral, and duplex, coils, scroll, and serpentine, line transect, a part for compound curve, and can extend with curved path.In some embodiments, as shown, dwell chamber 460 can be with one heart between the first chamber 405 and the 3rd chamber 408.The first chamber 405 can be configured in operation not containing ionogen and/or negative electrode sludge enriched material, and can be substantially as constraining in the space-filling between first end 440, inner anode 477 and baffle plate 450.The passage 462 that this space-filling first chamber 405 is roughly in dwell chamber 460 provides large radius, thereby increases total useful length and total surface area that passage 462 is exposed to the pressurized flow fluid electrolyte 53b wherein holding.The 3rd chamber 408 is as 42 temporarily keeping and/or carry waste cell melt fluid 53d to export 420 to one or more first from unit.In some embodiments, in order to reduce material cost, first end 440 can be configured to have the annular plate of the intermediate openings that is exposed to the first chamber 405, rather than the continuous plectane of shown solid.One or more the first outlets 420 can be arranged on to the top of unit 42, wherein overflow is tending towards more clarifying and does not contain negative electrode sludge enriched material.

Each passage 462 can be limited at least one anode 474, at least one negative electrode 472, and between the one or more isolators 476 that extend between it.Shown in embodiment in, one or more anodes 474 and one or more negative electrode 472 are provided as sleeve part, it is arranged alternately between anode 479 and inner anode 477 outside with one heart, wherein each sleeve part has different radii.Anode 474 and negative electrode 472 are radially spaced apart, and the interval being consistent by one or more spaced protrusions 473 of stretching out from described one or more negative electrodes 472.Although should be understood that not shownly, these one or more projections 473 can be alternatively only extended from anode 474, or can be from anode 474 and negative electrode 472 the two extension and not restriction.Yet, by provide projection 473 on one or more negative electrodes 472, provide extra cathode surface area in a small amount, for negative electrode sludge enriched material being precipitated out from pressurized flow fluid electrolyte 53b at electrolytic process.These one or more isolators 476 prevent the short circuit between the anode 474 of negative charge and the negative electrode 472 of positive charge, and can be used as flexible, tolerance compensating packing ring, it limits the cross-sectional boundaries of each passage 462 and in each passage 462, forms/concentrate pressurized flow electrolyte flow 53b.

As shown in Figure 18, each anode 474 can be communicated with one or more anode terminals 442.Anode terminal 442 can comprise, such as but not limited to, fastening piece 442a such as pin or bolt, such as nut, the clamp element 442b of flange or head, be connected to the terminal lead 442c of ground or power supply, conductive gasket 442d or other clamp element, prevent that electric current from flowing to the insulating sleeve 442e of peripheral part of unit 42, the fastening feature 442f that is arranged on the screw thread on fastening piece 442a or is equal to, comprise matching thread or for described screw thread or be equal to the conduction rack 442h that is equal to fastening feature 442g that fastening feature 442f engages, and be arranged in conduction rack 442h for engaging and support the receiving unit 442i of one or more anodes 474.Shown in embodiment in, anode 474 is cylindrical sleeves of tubulose substantially, and therefore receiving unit 442i can be set to little straight or arc slit roughly.Yet other is equal to and connects and can expect, especially for non-cylindrical or non-tubular shape anode 474 and negative electrode 472.For example, substitute slit, receiving unit 442i can comprise a plurality of conduction clamps, spring pinchcock, or the bolt extending from frame 442h, and it rides anode 474 and be fixed on it.

In some embodiments, this continuous electrolytic deposition system 40 ' can be provided with cylindrical unit body 406, and in flat circular, first end 440, and the second end 480 under cardinal principle conical butt.The frusto-conical of lower the second end 480 helps the heavy negative electrode sludge enriched material 53f collecting to be directed to the second outlet 430 for removing substantially.First end 440 can be fixed to cell body 406 by annular flange 445, and annular flange 445 can be electroneutral or positively charged together with cathode electrode unit body 406.First end 440 can comprise one group of plate folding, for example one or more ground connection or electric neutrality plate 447, one or more positive plates 444, and one or more insulcrete 446.In some embodiments, these one or more insulcretes 446 can comprise packing ring, for example polytetrafluoroethylene (PTFE) insulating washer.Can provide one or more fastening pieces 441 or tackiness agent first end 440 is fixed to body 406 and/or so that clamping plate 444,446,447 are fixed together.For example, one group of fastening piece 441 can be arranged on around first end 440, so that first end 440 is fixed to flange 445.For example fastening piece 441 can insulate by sheath, shell, sleeve or the packing ring of non-conducting material, and this non-conducting material is as High molecular weight polyethylene (HMWPE), polyvinyladine floride (PVDF), polypropylene, or polyvinyl chloride (PVC).In addition, fastening piece 441 can provide two objects that first end 440 is fixed to body 406 and also clamping plate 444,446,447 is fixed together.

In use, the inflow stream higher than the electrolyte solution 53 of environmental stress and temperature enters unit 42 continuously by entrance 410.Electrolyte solution 53 can contain the metal ion of copper, gold and silver, platinum, lead, zinc, cobalt, manganese, aluminium or uranium and not limit.This continuous electrolysis depositing system 40 ' preferably remain on temperature higher than environment (as, approximately 88 degrees Celsius) and/or pressure.The inflow stream of electrolyte solution 53 can hold tank (not shown) from upstream ionogen, elution system 20 ', or its combination continuously.In some embodiments, entrance 410 can be by having the pipe of one or more sidewalls 412 or a part for pipeline forms, and also can comprise the entrance frame 414 that there is flange, sealing member, valve, pipe fitting or be equal to web member, for continuous elution system 20 ' combination.Entrance 410 comprise one or more opening 413(as, by described one or more sidewalls 412), it is configured to enter electrolyte solution 53 to one or more passages 462 feedings of dwell chamber 460.Although not shown, can be each passage 462 a plurality of openings 413 are provided.In the situation that using as shown a plurality of passages 462 and single entrance 410, electrolyte solution 53 streams of inflow can be divided into the inflow stream 53a that multiply is disperseed, and respectively enter different passage 462.Alternatively, although not shown each passage 462 that can be provides independent entrance 410.Opening 413 can be configured to provide consistent or inconsistent velocity of flow at each passage 462, or provides the similar ionogen residence time for each passage 462.As Figure 17 is clearly shown that, can be by one or more isolator 417(as, insulating mat) be arranged between one or more sidewalls 412 of entrance 410 and the first end 440 of cell body 460.These one or more isolators 417 can enter electrolyte solution 53 not in opening 413 with what guarantee to become a mandarin 53a from dispersion train around one or more openings 413, particularly with negative electrode 472 adjacent formation, plating or sludge.

In some embodiments, passage 462 can be configured to allow the dispersion train of electrolyte solution 53 53a that becomes a mandarin be forced to flow by passage 462 with pressurization fluid electrolyte 53b, and this pressurization fluid electrolyte 53b is as shown in the figure along consistent spiral or the path of spiraling.Yet, although not shown, passage 462 also can be configured to along straight path, serpentine path, compound curve path or compound 3D SPL path and guide the incoming fluid 53a of dispersion, as long as passage can support pressurized stream fluid electrolyte 53b therein, and provide the sufficient residence time of ionogen between anode 474 and negative electrode 472.

When they extend in dwell chamber 460, passage 462 can shrink or extend in periphery, or can in total or shape of cross section and/or size, change; Yet preferably passage 462 is consistent at cross section, direction and/or anode-cathode interval in whole length along it.Although not shown, longer and by the more residence time of passage 462 substantially having relatively owing to being positioned at passage from the larger radial distance in 42 center, unit, so compared with interior passageway 462(as, with the passage adjacent with the first chamber 405 compared with inner anode 477) the number of turns can be adjusted to comparison exterior passage way (as, more approach the passage of outer anode 479 and the 3rd chamber 408) the number of turns more.In other words, although not shown, the height of the interior part of dwell chamber 460 can be greater than the outer part of dwell chamber 460, thereby it is adjacent with the first chamber 405 to lengthen interior passageway 462() useful length.Baffle plate 450 parts adjacent with the 3rd chamber 408 with dwell chamber 460 are opened substantially, thereby allow passage 462 carry continuously waste cell melt stream 53d to the three chambers 408, and the collection negative electrode sludge enriched material 53f forming in passage 462 is delivered to the second chamber 407.

As shown in Figure 16, baffle plate 450 can comprise anode layer 452, supports the middle electric neutrality isolator 454 of described one or more anode 474 and negative electrode 472, and for the supporting structure 456 of support insulator 454 and anode layer 452.This isolator 454 can be made by the chemical robust material such as ultrahigh molecular weight polyethylene(UHMWPE) (UHMWPE), and the cross shown in can being (cruciform) shape.A plurality of receiving units 458 such as recess can be arranged in isolator 454 with the one or more anodes 474 of maintenance, interval, insulation and support and negative electrode 472; Yet, other holding devices such as bolt, spring pinchcock or clamp can be provided.Isolator 454 can be connected to supporting structure 456 by one or more fastening pieces, tackiness agent or other coupling device, and supporting structure 456 can be by connecing such as fastening, shaping, bonding, weld or be supported on flange or the first-class usual manner of frame is connected to body 406.Anode layer 452 can be used for closing the first chamber 405, and prevents that the ionogen 53 in pressurized flow electrolyte flow 53b from entering described the first chamber 405.In some embodiments, supporting structure 456 can be the trellis as mesh screen, or as the supporting structure of cross bar, cross bar crosses the width of cell body 406.Supporting structure 456 is configured to not stop the ionogen that flow to the 3rd chamber 408 from passage 462 substantially, or stops passing through to the negative electrode sludge enriched material 53f of the second chamber 407.

Electrolyte solution 53 pressurization ground flow through the one or more passages 462 in dwell chamber 460, large electromotive force is arranged between one or more anodes 474 and one or more negative electrode 472, thereby sludge enriched material " is separated out to (plate-out) " effectively to one or more negative electrodes 472.Yet, by changing the operating parameters such as the smoothness/material/coating of the residence time, electric current, electrolyte flow speed, temperature, pressure, electrolyte concentration/composition and/or each negative electrode 472 etc., passage 462 can be configured to make negative electrode sludge enriched material be initially formed on one or more negative electrodes 472 or be adjacent, but will be not can actual bonding or " coating is to (plate) " negative electrode 472, but sweep away passage 462 and/or become, be suspended in pressurized flow fluid electrolyte 53b.Any sludge enriched material that can be deposited on the bottom of passage 462 also can be rinsed downwards and last pressurized flowing electrolyte fluid 53b scans out passage 462 and enters the second chamber 407.Sludge enriched material can be rushed out one or more passages 462 in the following manner: act on the gravity on inclined surface, pressurized flow fluid electrolyte 53b is by the high flow rate of one or more passages 462, the turbulent flow of the increase in each passage 462, and/or by being arranged on the little transverse cross-sectional area on each passage 462.

After pressurized flow fluid electrolyte 53b passes through one or more passages 462, the outflow stream 53c of dwell chamber 460 will comprise liquid bearing part and the solid precipitation part of lean solution 54 substantially, liquid bearing part does not have the precious metal dissolving substantially, and solid precipitation partly comprises the negative electrode sludge enriched material of discharging from passage 462 by pressurized flow fluid electrolyte 53b.Heavier solid was followed precipitation deposition flow stream 53e precipitate the negative electrode sludge enriched material 53f that becomes a large amount of accumulations in the second chamber 407 adjacent with the second end 480 before.Lean solution 54 moves into the 3rd chamber 408 via waste cell melt fluid 53d, and via outlet 420, leaves unit 42 constantly.In some embodiments, wherein cell body 406 is negative electrodes, and some residues are electroplated or negative electrode sludge enriched material forms and can appear in the 3rd chamber 408 (for example,, in the interior part of cathode side walls 482 or around the interior part of cathode side walls 482).Yet any any negative electrode sludge enriched material 53f being formed in the 3rd chamber 408 will deposit conventionally, and last play in the second chamber 407 with all the other accumulation negative electrode sludge enriched material 53f mono-.

The first outlet 420 can be by having the pipe of one or more sidewalls 422 or a part for pipeline forms, and also can comprise the first export frame 424, the web member that is equal to that it comprises flange, sealing member, valve, pipe fitting or is bonded to continuous elution system 20 '.In use, the outflow of lean solution 54 is flowed through and is left constantly cell body 406 by described the first outlet 420, and it can enter lean solution maintenance tank (not shown) at this, to export 420 places, goes out of use, and is back to continuous elution system 20 ', or is further processed.

The negative electrode sludge enriched material 53f obtaining can be via the second opening 430 42 removes from unit off and on or constantly.The underflow of negative electrode sludge enriched material 53f or sludge remove stream 53g can advance to maintenance tank, be pumped and leave or further purify, or can be to container and be delivered to smelting furnace.In some embodiments, the second outlet 430 can be by having the pipe of one or more sidewalls 432 or a part for pipeline forms and also can comprise the second export frame 434, and it has flange, sealing member, valve, pipe fitting, nozzle, tap or for being bonded to the web member that is equal to that holds tank or smelting apparatus.

The cross section of this dwell chamber 460 can change, as long as one or more passage 462 is formed between at least one anode 474 and at least one negative electrode 472, at least one anode 474 and at least one negative electrode 472 are spaced apart from each other by one or more isolators 476.A plurality of " 8-shaped " connection, horizontally disposed and vertical displacement with series connection, or with any continuous path in the 3-D space of any " pressurized flow " that is configured to provide electrolyte solution, passage can linear (similar elongate tube), extend spirally.In order to help that the air blocking in passage 462 is removed, and also prevent that the deposition sludge enriched material in passage from stopping up, preferably in 3d space, the continuous path of mobile passage does not have sharp turn, unexpected turning, pendant, protuberance, and/or the tight corner of coiling, these can be tending towards air and block and obtain and block.In some embodiments, dwell chamber 460 can comprise one or more passages 462, and it only extends as being inclined relative to the horizontal to the long straight pipeline section of an angle.

Figure 19 is schematically illustrated according to the continuous electrolysis depositing treatment 40 of some embodiments.This processing 40 comprises the electrolyte solution 53 that 1082 temperature and pressures higher with respect to ambient conditions are provided.Electrolyte solution 53 can be processed 20 by continuous wash-out and produce, and wherein can comprise water, prussiate, caustic alkali and dissolution of metals (as, gold, copper, silver, platinum, aluminium, lead, zinc, cobalt, manganese or uranium).Electrolyte solution 53 continuously feeding 1084(as, with predetermined velocity of flow) to continuous ionogen metals recovery units 42, it preferably keeps 1086 than the higher temperature of environment and/or pressure.In some embodiments, unit 42 can comprise one group of nested anode lug 474 and cathode sleeve 472, and wherein adjacent sleeve has different electromotive forces or electric charge.In a preferred embodiment, this sleeve is relative to each other evenly spaced apart with one heart and radially, thereby any two adjacent sleeves keep contrary electric charge 1088.One or more isolators 476 can be arranged between anode 474 and negative electrode 472, to limit a plurality of passage 462(as, spirality channel), and prevent the electric discharge between anode and negative electrode simultaneously.Processing 40 also comprises allows electrolyte solution 53 experience for the 1090 longer residence time in continuous electrolysis matter metals recovery units 42.This can be by providing one or more elongate channel 462 to realize between anode 474 and negative electrode 472 sleeves, and it can smoothly, continuously and not interrupt spiral path and extends.Should be understood that also can be by adopting the long straight passage of tubulose to increase the residence time alternatively.By the little pressure difference between the little pressure difference between entrance 110 and the one 120 outlet and/or entrance 110 and the 2 130 outlet, electrolyte solution 53 pressurizations that remain in passage 462 are passed through to passage 462 and Qi Bi.Along with electrolyte solution 53 moves through passage 462, negative electrode sludge enriched material deposits from electrolyte solution 53, until strength of solution is thinning and finally substantially do not contain exotic material 1092.Deposition enriched material from sludgy deposits stream 53e is collected 1094 constantly in the second chamber 407, and the negative electrode sludge enriched material 53f collecting can be by continuously or off and on or both are combined extracts 1098.It does not have rare metal substantially lean solution 54() flow through and from unit, 42 extract continuously 1096 by outlet 420, and can in processing 20, be fed to continuous wash-out container 24 at wash-out continuously.

Figure 20 illustrates the charcoal manipulation of regeneration 30 according to some embodiments.The solid part 55 that comprises the thickened waste slurry 51d of the useless charcoal that anhydrates sieves to isolate useless carbon powder 55b by screen cloth 32.This useless carbon powder 55b is placed on carbon powder to be held in tank 34.Remaining thick (course) useless charcoal 55a be sent to regeneratory furnace 35(or for regenerating as other device of chemical, steam or biological treatment).Hot reactivate charcoal 55c is removed from regeneratory furnace 35, and quench in charcoal quench drum 36.Cooling regenerated carbon and the slurry of fluid move to dehydration screen cloth 37 via pump 33.After by dehydration screen cloth 37, the activity/regenerated carbon 56 of dehydration moves to continuous carbon loading/adsorption treatment 70.This fluid underflow that comprises cold reactivate charcoal slurry 55d, is moved into carbon powder and holds tank 34.

Figure 21 shows continuous metal extraction system 100 ' according to certain embodiments of the present invention, and it comprises continuous pickling system 10 ', continuous elution system 20 ', continuous electrolysis depositing system 40 ', and charcoal regeneration system rapidly 30 '.Figure 22 and 23 is for comparing ratio equipment layout and whole floor space.Figure 22 shows for according to the system 100 ' of the continuous extraction metal of Figure 21, and Figure 23 comprises for carry out the conventional system 9000 ' of the batch extracting of metal by " in batches " treatment step.As can be from as shown in Figure 22 and 23, less than the conventional system 9000 ' shown in Figure 23 according to the size of system 100 ' of the present invention.Except smaller szie, system 100 ' also can be more effectively and environmental friendliness more.

Figure 24 shows the washing tank 200,200 ', 200 shown in Fig. 6-8 " optional embodiment.In the embodiment shown, provide pickling tank 2000, its replaceable pickling tank 200.Pickling tank 2000 comprises washing chamber 2020, it has fluidized bed board 2021, one or more adjustable articulators 2007, 2009, be arranged on the recirculation entrance 2023a of fluidized bed board 2021 belows, with the recirculation outlet 2023b that is arranged on fluidized bed board 2021 tops, wherein said fluidized bed board 2021 is crossed over the length of washing chambers 2020 and is had than the less hole dimension of the average particle size particle size of material containing charcoal of material containing/again, described one or more adjustable articulator 2007, 2009 can raise individually, reduce or go up pivotable to change chamber 2020 with respect to the angle of inclination of slideway 2002 at tooth bar or connection mechanism's (being that clearly object is not shown).Recirculation outlet 2023b comprises one or more overflow outlets 2027, and it is respectively provided with at least one and can washs/replaceable recirculation screen cloth 2008, and it is by material containing/material containing charcoal 57 remains in chamber 2020 and filters existing dilute acid solutions 57c again.Recirculation screen cloth 2008 can be arranged between the screw flange element of overflow outlet 2027 easily, and can comprise built-in circumferential gasket.Figure 25 and 26 shows the view of the more details of the chamber 2020 shown in Figure 24.

Recirculation entrance 2023a can comprise for making the one or more adjustable nozzles 2011 of material containing charcoal 57 fluidisations of material containing/again.This nozzle 2011 can be by angular adjustment individually or jointly, and " setting " is to fixed angle, thereby: the difference of compensation chamber 2020 tilts, and prevents material containing/accumulation of material containing charcoal 57 again, and resists the backflow in the chamber 2020 causing around the eddy current of Internal baffle 2018.As shown, chamber 2020 can be configured to clam shell form, and wherein a plurality of fastening pieces 2004 partly link together upper and lower clam shell.Can by one or more other gasket applications between upper and lower clam shell part to form sealing, but or fluidized bed board 2021 self be provided with perimeter gasket material behavior partly to provide sealing at upper and lower clam shell.

The first strainer 2001 is arranged on to the entrance 2022 of pickling tank 2000.The first strainer 2001 comprises housing 2003, be used for collecting the material containing charcoal slurry 57 ' of inflow material containing/again, for by the material containing charcoal 57 of material containing/again from the first screen cloth 2026 of the carrying object 57f separation of slurry 57 ', be used for the material containing of filtration/material containing charcoal 57 is delivered to the first filtering outlet 2006 of washing chamber 2020 from upper housing 2003 again, collection is from the recirculation tank 2029 of the carrying object 57f of the liquid portion separation of inflow slurry 57 ', and one or more clamps 2005, it is removably connected to recirculation tank 2029 by housing 2003, and be extended with the first screen cloth 2026 therebetween, thereby allow periodically to clean and/or change the first screen cloth 2026.Recirculation tank 2029 can be configured to delivery fluid 57f to be redistributed to continuously and to hold tank (not shown), or can only comprise for removing in batches the valve of the carrying object 57f of collection.

Second strainer 2024 similar to the first strainer 2001 is configured to adjacent with first channel 2082, and this first channel 2082 extends to the Outboard Sections of washing chamber 2020 from fluidized bed board 2021.First channel 2082 be configured to acid rinse material containing charcoal 57a in chamber 2020 through after the predetermined pickling residence time, the discharge of the pickling material containing charcoal 57a of provide from fluidized bed board 2021/around/top.This acid rinse material containing charcoal 57a is filtered by the second screen cloth 2036, and the solid part after the filtration of acid rinse material containing charcoal 57a is discharged from discharging outlet 2028.From discharging these acid rinse material containing charcoals that outlet 2028 discharges, can be received tank 2060 and block and obtain and keep, and be delivered to subsequently (via pump 2030) downstream processing (as, water rinse circulation).Alternatively, from discharge acid rinse material containing charcoals that outlet 2028 discharges can directly enter downstream processing (as, pour another water rinse tank 200 ' into, and hold tank 2060 and pump 2023 without centre).Holding tank 2060 is advantageously used for the level of maintenance processing controls and prevents that too much charcoal is fed to the buffering of downstream processing.

In use, supplementary dilute acid solutions 57c ' (by utilizing the second screen cloth 2036 filter acid rinsing material containing charcoal 57a to obtain) enters recirculation tank 2039, and is pumped to chamber 2020 by pump 2030.This supplementary dilute acid solutions 57c ' enters recirculation entrance 2023a, and then via nozzle 2011, upwards passes through fluidized bed board 2021.This supplementary dilute acid solutions 57c ' makes that the material containing that enters/material containing charcoal 57 suspends again, and the material containing charcoal 57 of material containing/is again moved through to chamber 2020 and around baffle plate 2,011 one predetermined parking times.This supplementary dilute acid solutions 57c ' moves through recirculation screen cloth 2008, and the dilute acid solutions 57c after filtering exports 2033b by recirculation and enters recirculation tank 2039 again.Can be by regulating the angle of inclination of chamber 2020 and/or regulating the angle direction of nozzle 2011 to extend or shorten the residence time of material containing charcoal 57 of material containing/again.For fixing, immutable METAL EXTRACTION, process, the position, angle of the angle of inclination of chamber 2020 and nozzle can be preset by producer, and is for good and all fixed on best configuration to produce the most effective residence time of described processing.

Example 1

Comprise about 30-300 ounce/ton gold and the water base material containing charcoal slurry 57 of 30%wt/wt roughly, active palm shell charcoal is transported to continuous pickling system 10 '.First, by comprise about 1-5wt% hydrogenchloride (HCl) and/or nitric acid (HNO in pickling tank 12,200 ₃) dilution water acid solution the active-carbon bed fluidisation of material containing is removed inorganic components (that is, calcium and magnesium acid calcium) from material containing charcoal.This material containing gac is delivered to water rinse tank 14,200 ' constantly from pickling tank, and wherein material containing gac is fluidized and cleans with water.Subsequently, this material containing gac is delivered to caustic alkali rinse tank 16,200 constantly from water rinse tank 14,200 ' ".By comprising that roughly the caustic solution of 1-3wt% sodium hydroxide rises to the pH value that is delivered to the material containing gac of caustic alkali rinse tank more than 10.

This basic de-sludging material containing charcoal 50 is by comprising the delivery medium of the caustic alkali elution solution of 1wt% caustic alkali (NaOH) and 0.1wt% prussiate (NaCN) roughly and being fed to constantly the ejecting container 22 in continuous elution system 20 '.Ejecting container 22 is roughly maintained at about 100 and 200 Fahrenheit degree (℉) between working temperature, and at the pressure of atmospheric level roughly.This material containing charcoal is delivered to continuous wash-out container 24 from ejecting container 22, and wherein gold is removed (that is, gold dissolves) from charcoal.This continuous wash-out container 24 is at about 300 Fahrenheit degree (℉) work, this temperature is by rising to elution solution pressure about 70psi(standard) realize.Wash-out container 24 is expelled to overdraft ejecting container 25 constantly continuously.Pressure decreased between wash-out container 24 and ejecting container 25 makes to discharge the quick flash vaporization of a part of caustic alkali elution solution continuously.The steam producing is directed to ejecting container 22, thereby heats ejecting container 22 and cooling flash chamber 25 simultaneously.Useless charcoal (as, comprise and be less than 1 ounce of/ton of gold) from continuous elution system 20 ', removed and entered manipulation of regeneration 30.

Roughly 300 ℉ pressurization caustic alkali elution solutions filter by one or more screen clothes or strainer 324, and to remove useless charcoal particle and to form electrolyte solution 53, it is then by continuous electrolysis matter METAL EXTRACTION (that is, electrolytic deposition) unit 42.This electrolyte solution 53 pressurized (pressure of the increase providing by continuous wash-out container 24) is by least one passage 462, and it has the fixedly spiral path between cylindrical sleeves anode 474 and cylindrical sleeves negative electrode 472.Roughly the voltage between 2 and 4 volts passes through between anode 474 and negative electrode 472 via electrolyte solution 53, thereby negative electrode sludge enriched material 53f is deposited on to the surface of negative electrode 472.The speed of electrolyte solution 53 forms forced-flow electrolyte flow 53b in passage 462, its negative electrode sludge enriched material 53f of accumulation that can form and accumulate in constantly the cathode surface of unit 42 rinses to conical lower portion, and wherein it can remove at one's leisure or remove constantly by control valve operator.

Contractor or other entities can provide system 100 ' or process 100, for partly or entirely as shown or illustrated continuous extraction metal.For example, contractor can receive the bid requirement that relates to design continuous metal extraction system 100 ' or process 100 project, or contractor can be provided as client's design such as system 100 ' or process 100.Then contractor can provide illustrated any one or more devices or feature in the as directed and/or above-mentioned embodiment of example.Contractor can be by selling this device or providing described device by this device of offering for sale.Contractor can provide numerous embodiments, and it is arranged by size, and shape forms and/or be additionally configured to meet specific client or client's design conditions.Contractor can subcontract device or for manufacture, conveying, sale or the installation of parts of other device of described device is provided.Contractor also can investigate scene and designs or specify one or more storage areas for the stacking material that is used for manufacturing installation.The device that contractor also can keep, revises or upgrade and provide.Contractor can be by this device of subpackage or by being directly provided for described maintenance or revising needed service or parts provide this maintenance or modification, and in some cases, contractor can by " renovation suit " revise existing METAL EXTRACTION process 9000 or system 9000 ' to realize process or the transmission device system of modification, it comprises system described here 100 ' and processes 100 one or more method stepss, device or feature.

Although described the present invention with concrete embodiment and application, yet those of ordinary skills can obtain other embodiment and modification and not depart from the desired essence of the claims in the present invention or exceed its scope under described instruction.For example, the particle except charcoal and carrier (as, polymkeric substance or ion exchange resin) can be used for system of the present disclosure and processing.In addition, the reagent except water, prussiate and caustic alkali can be used for washing, de-sludging or elution particle.In addition, disclosed system and processing can be used for extracting multiple material, include but not limited to copper, gold and silver, platinum, uranium, lead, zinc, aluminium, chromium, cobalt, manganese, rare earth element and basic metal etc.Therefore, the accompanying drawing that should understand here provides with the mode of explanation with example, to contribute to the understanding of the present invention, and should not form restriction on its scope.

Reference numeral

10 continuous picklings are processed

10 ' continuous pickling system

12 pickling tanks

13 pumps

14 water rinse tanks

16 alkali rinse tanks

20 continuous wash-outs are processed

20 ' continuous elution system

21 fluid circuits

22 ejecting container

23 pumps

24 continuous wash-out containers

25 flash chambers

26 dehydration screen clothes

27 immersion heaters

28a flows into manifold

28b flows out manifold

29 valves

30 charcoal manipulation of regeneration

30 ' charcoal regeneration system rapidly

32 screen clothes

33 pumps

34 carbon powders hold tank

35 regeneratory furnaces

36 charcoal quench drum

37 dehydration screen clothes

40 continuous electrolysis depositing treatment

40 ' continuous electrolysis depositing system

42 continuous electrolysis matter METAL EXTRACTION unit

50 de-sludging material containing charcoals (or its alkali/basic slurry)

The slurry of 51 elution solutions and de-sludging material containing charcoal

51a heating and/or add grouting material

The sinuous flowing-path of 51b slurry

51c waste slurry

51d thickened waste slurry

The liquid portion of 52 thickened waste slurries

53 electrolyte solutions

53a disperses incoming fluid

53b pressurized flow fluid electrolyte

53c dwell chamber flows out

53d waste cell melt stream

53e sludgy deposits stream

53f negative electrode sludge enriched material

53g deposition removes stream

54 lean solutions (that is, waste electrolyte)

The solid part of 55 thickened waste slurries (that is, dehydration)

The thick useless charcoal of 55a

The 55b carbon powder that gives up

The hot reactivate charcoal of 55c

The cooling reactivate charcoal of 55d slurry

56 activation/reactivate charcoals

The material containing charcoal slurry of 57 ' material containing/again

The material containing charcoal of 57 material containings/again

57a acid rinse material containing charcoal

57c, 57c ' dilute acid solutions

57d, 57d ' water rinse solution

57e alkali rinsing solution

57f carries fluid

60 hold tank

70 continuous carbon loading/adsorption treatment

70 ' continuous carbon loading/adsorption system

100 processing of extracting for continuous metal

100 ' the system of extracting for continuous metal

200 pickling tanks

200 ' water rinse tank

200 " alkali rinse tank

220 first chambers

221 first class bed boards

222 first entrances

223a the first recirculation entrance

223b the first recirculation outlet

224 first overflow weirs

226 first screen clothes

227 first overflow outlets

228 first discharge outlet

229 first recirculation tanks

230 second chambers

231 second fluidized bed boards

232 second entrances

233a the second recirculation entrance

233b the second recirculation outlet

234 second overflow weirs

236 second screen clothes

237 second overflow outlets

238 second discharge outlet

239 second recirculation tanks

240 the 3rd chambers

241 the 3rd fluidized bed boards

242 the 3rd entrances

243a the 3rd recirculation entrance

243b the 3rd recirculation outlet

244 the 3rd overflow weirs

246 the 3rd screen clothes

247 the 3rd overflow outlets

248 the 3rd discharge outlet

249 the 3rd recirculation tanks

251 sour overflows

253 discharge sour loop

254 rinse water overflows

256 discharge rinse water loop

257 alkali rinsing overflows

260 diapires

266 interior tubular walls

268 outer tubular wall

282 first channels

284 second passages

286 third channels

57b rinsing material containing charcoal

301 inlet seal parts

302 entrance framves

304 entrances

306 first ends

308 second ends

310 one or more sidewalls

312 relief outlet framves

314 installation elements

316 relief outlets

318 one or more baffle plates

320 fluidized bed boards

322 influx framves

324 strainers (as, disk screen)

326 influxs

328 outlets

329 exit seal parts

330 export frames

340 dwell chamber

350 fluidisation chambers

402

404

405 first chambers

406 cell body

407 second chambers

408 the 3rd chambers

410 entrances

412 one or more entrance sidewalls

413 one or more openings

414 entrance framves

417 one or more isolators

420 first outlets

422 one or more the first outlet sidewalls

424 first export frames

430 second outlets

432 one or more the second outlet sidewalls

434 second export frames

440 first ends

441 fastening pieces

442 anode terminals

442a fastening piece

442b clamp

442c terminal lead

442d conductive gasket

442e insulating sleeve

442f screw thread or be equal to fixed character

442g coupling screw thread or fixed character

442h conducting bracket

442i receiving unit

444 positive plates

445 cathode flanges

446 insulcretes

447 positive plates

450 baffle plates

452 positive plates

454 anode/cathode isolators

456 anode/cathode insulating frames

458 one or more receiving units

460 dwell chamber

462 one or more passages

472 negative electrodes

473 one or more projections

474 anodes

476 one or more isolators

477 inner anodes

479 outer anodes

480 second ends

482 one or more sidewalls

1000 for reclaiming continuously the processing of metal

1002-1046 continuous pickling step

The continuous elution step of 1048-1080

1082-1100 continuous electrolysis deposition step

2000 pickling tanks

2001 first strainers

2002 stands

2003 housings

2004 fastening pieces

2005 clamps

2006 first filter outlets

2007 first adjusting brackets

2008 recirculation screen clothes

2009 second adjustable articulators

2011 nozzles

2018 baffle plates

2020 chambers

2021 fluidized bed boards

2022 entrances

2023 pumps

2023a recirculation entrance

2023b recirculation outlet

2024 second strainers

2026 first screen clothes

2027 overflow outlets

2028 discharge outlet

2029 recirculation tanks

2033b recirculation outlet

2036 second screen clothes

2039 recirculation tanks

2060 hold tank

2082 first channels

9000 conventional batches of metal recyclings

The 9000 ' conventional batches of metal recovery system

9100 conventional cleanup acid treatment in batches

9100 ' conventional pickling system in batches

9120 pickling containers

9132 pumps

9134 charcoal transferpumps

9136 pumps

9140 dilute acid tanks

9150 pond pumps

9160 neutralizing wells

9200 conventional (Zha Dela elution (Zadra strip)) wash-outs are in batches processed

9200 ' conventional (Zha Dela elution) elution system in batches

9220 lean solution tanks

9232 charcoal transferpumps

9234 lean solution stand-by pumps

9236 lean pumps

9237 lean solutions

9239 hot lean solutions

9240 elution containers

9250 heat stands or are equal to heat exchanger

9300 charcoal manipulation of regeneration

9400 conventional electrolytic depositions are in batches processed

9400 ' conventional electrolytic deposition system in batches

9420 batch ionogen METAL EXTRACTION unit (as, removable plate negative electrode)

9421 thermal electrolysis matter solution

9430 pumps

9440 electrolytic deposition pump boxes

9500 de-sludging material containing charcoals

9530 electrolyte solutions

9540 lean solutions

9550 useless charcoals

9560 activity/reactivate charcoal

9570 material containings or again material containing charcoal

9700 conventional charcoal loading processing in batches

Claims (17)

1. the system [100 '] for the continuous recovery of metal, comprise following at least one:

Continuous pickling system [10 '], it is configured for and receives inflow continuous, unbroken material containing carbon particles [57], and the outflow of carrying continuous, unbroken de-sludging material containing carbon particles [50];

Continuous elution system [20 '], it is continuous that it is configured for reception, the inflow of unbroken elution solution [51] that comprises de-sludging material containing carbon particles [50], and carry continuously the outflow of unbroken electrolyte solution [53]; With

Continuous electrolysis depositing system [40 '], it is configured to receive continuous, and the outflow of continuous unbroken lean solution [54] is carried in the inflow of unbroken electrolyte solution [53], and does not interruptedly form continuously negative electrode sludge enriched material [53f];

Wherein said continuous pickling system [10 '], described continuous elution system [20 '], and each of described continuous electrolysis depositing system [40 '] is configured to work simultaneously, and do not have conventional batches of metal to recycle total interruption.

2. the system as claimed in claim 1 [100 '], also comprises the charcoal regeneration system rapidly [30 '] that may be operably coupled to described continuous elution system [40 '].

3. the system as claimed in claim 1 [100 '], also comprises the continuous carbon loading/activation system [70 '] that may be operably coupled to described continuous pickling system [10 '].

4. the system as claimed in claim 1 [100 '], also comprises being operatively coupled on and holds tank [60] between described continuous pickling system [10 '] and described continuous elution system [20 '].

5. the system as claimed in claim 1 [100 '], comprises described continuous pickling system [10 '], described continuous elution system [20 '], and in described continuous electrolysis depositing system [40 '] whole three.

6. the system as claimed in claim 1 [100 '], also comprises one or more pumps [13,23,33].

7. the system as claimed in claim 1 [100 '], wherein said continuous elution system [20 '] may be operably coupled to described continuous electrolysis depositing system [40 '].

8. system as claimed in claim 7 [100 '], wherein elution system [20 '] also comprises one or more screen clothes or strainer [324] continuously, and described screen cloth or strainer [324] are configured to prevent that carbon particles is transported to described continuous electrolysis depositing system [40 '].

9. the system as claimed in claim 1 [100 '], wherein said continuous pickling system [10 '] also comprises the chamber [220] that is suitable for holding fluidizing medium; Be suitable for receiving the entrance [222] of the charging that contains material containing carbon particles [57]; Be suitable in the situation that there is described fluidizing medium fluidized-bed distribution plate [220] or other device of material containing carbon particles [220] described in fluidisation; Be suitable for carrying from described chamber the outlet [228] of material containing carbon particles and fluidizing medium; With the screen cloth [226] that is suitable for filtering from fluidizing medium material containing carbon particles;

Wherein said continuous elution system [20 '] comprises ejecting container [22], continuous wash-out container [24], and flash chamber [25], wherein said ejecting container [22] is operationally connected to described continuous wash-out container [24], described continuous wash-out container [24] is operationally connected in series to described flash chamber [25], and described ejecting container [22] is operationally connected to described flash chamber [25] abreast; And

Wherein said continuous electrolysis depositing system [40 '] comprises continuous electrolysis matter metals recovery units [42], and described continuous electrolysis matter metals recovery units [42] has the cell body [406] that is configured to electrolyte solution [53] to remain on high pressure and/or high temperature, at least one anode [474], at least one negative electrode [472], be configured to receive the entrance [410] that continuously, interrupt flow does not become a mandarin of electrolyte solution [53], be configured to discharge continuously, do not interrupt the first outlet [420] that lean solution [54] flows out stream, be configured to remove the second outlet [430] of negative electrode sludge enriched material [53f], and dwell chamber [460], described dwell chamber [460] is configured to carry continuously electrolyte solution [53] to described the first outlet [420] from described entrance [410], and increase the residence time of described electrolyte solution between at least one anode [474] and described at least one negative electrode [472], described dwell chamber [460] comprises one or more passages [462], described one or more passage [462] is configured to provide therein the pressurized stream of electrolyte solution [53], it is enough by force to evict continuously and/or to carry negative electrode sludge enriched material the final described dwell chamber [460] of discharging from along described one or more passages [462].

10. the system as claimed in claim 1 [100 '], wherein said continuous pickling system [10 '] also comprises dilute acid solutions [57c], water rinse solution [57d], and at least one in caustic alkali rinsing solution [57e]; Wherein said continuous elution system [20 '] also comprises the solution that contains following at least one: be loaded with the carbon particles of precious metal, electrolyte solution, useless carbon particles, caustic alkali, water-based composition and prussiate; And wherein said continuous electrolysis depositing system [40 '] also comprises electrolyte solution.

11. the system as claimed in claim 1 [100 '], wherein said continuous pickling system [10 '], described continuous elution system [20 '], and described continuous electrolysis depositing system [40 '] be respectively configured to the raise solution wherein hold or pressure and/or the temperature of slurry.

12. the system as claimed in claim 1 [100 '], wherein charcoal regeneration system rapidly [30 '] may be operably coupled to described continuous elution system [20 '], continuous carbon loading/activation system [70 '] may be operably coupled to described continuous pickling system [10 '], and described charcoal regeneration system rapidly [30 '] may be operably coupled to described charcoal loading/activation system [70 '].

13. the system as claimed in claim 1 [100 '], wherein said continuous pickling system [10 '] may be operably coupled to described continuous elution system [20 '].

14. 1 kinds of methods for the continuous recovery of metal [100], comprising:

To continuous washing system [10 '] feeding continuously [1004], be loaded with the particle [57] of metal;

In described continuous washing system [10 '] continuously washing [1006,1020,1034] described material containing particles [57] with by the de-sludging of described material containing particle;

From described continuous washing system, remove continuously [1046] de-sludging material containing particle [50];

To continuous elution system [20 '], load continuously [1050] described de-sludging material containing particle [50];

From described continuous elution system [20 '], remove continuously [1064] electrolyte solution [53];

To continuous electrolysis depositing system [40 '] feeding continuously [1066,1082,1084] described electrolyte solutions [53];

From described continuous electrolysis depositing system [40 '], remove continuously [1070,1096] lean solution [54]; With

Carry continuously [1072] to described continuous elution system [20 '] described waste cell melt solution;

Wherein said continuous washing system [10 '], described continuous elution system [20 '], and each in described continuous electrolysis depositing system [40 '] is operably connected and is configured to allow above-mentioned steps to carry out simultaneously.

15. methods as claimed in claim 14 [100], also comprise by the continuous loading/adsorption system [70 '] identical with described continuous washing system [10 '] continuously adsorbing metal form described material containing particle to described particle.

16. methods as claimed in claim 15 [100], wherein said particle is a kind of in carbon particles, polymer absorbant or ion exchange resin.

17. methods as claimed in claim 14 [100], also comprise from described continuous electrolysis depositing system [40 '] and remove continuously [1098] negative electrode sludge enriched material [53f].

Images