CN205099491U - Device of concentrated separation washing ore pulp of membrane separation - Google Patents
Device of concentrated separation washing ore pulp of membrane separation Download PDFInfo
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- CN205099491U CN205099491U CN201520827232.4U CN201520827232U CN205099491U CN 205099491 U CN205099491 U CN 205099491U CN 201520827232 U CN201520827232 U CN 201520827232U CN 205099491 U CN205099491 U CN 205099491U
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Abstract
The utility model relates to a device of concentrated separation washing ore pulp of membrane separation belongs to the hydrometallurgy field. The device is including membrane filter, and including box, deposit room among the membrane filter, the deposit room sets up in the below of box, has at least one film element at box internally mounted, the inside of film element set up an at least penetrant passageway, the outside of film element is provided with the opening of penetrant passageway, is provided with sealed head at the opening part, sealed head separates the hold back side of opening with dull and stereotyped film element, is produced from mouth of a river to at least one sealed overhead film element that is provided with, be provided with the aeration pipe in the below of film element, still be provided with feed inlet and air supply pipe on the box. The utility model provides a terminal formula diffusion barrier filtration system is the core, through little crossflow filtration of malleation or negative pressure suction filtration, has ensured the serialization production of the concentrated separation of ore pulp, the passing through gases malleation squeeze with the aqueous vapor agitator treating, improved the metal ion's in the ore pulp the rate of recovery, reduced investment and running cost.
Description
Technical field
The utility model relates to a kind of device of membrane separation concentration separating, washing ore pulp, relates in particular to a kind of technique adopting terminal type ceramic membrane filter equipment concentrating and separating to wash ore pulp, belongs to field of hydrometallurgy.
Background technology
In hydrometallurgy process, ore pulp adds after soda acid Fusarium Wilt of Sweet goes out, and need carry out the solid-liquid separation between leach liquor and slag, to obtain the leach liquor containing valuable metal ions, carry out next process deep processing.This ore pulp has following feature: 1, in ore pulp, solid content is larger, reaches 10 ~ 15%.Admittedly containing thing except the slag that Leaching reaction does not occur, also containing the more suspended solids generated by Leaching reaction.This suspended solids adds density and the viscosity of ore pulp on the one hand, hinders the sedimentation of slag; The porosity and looseness of suspended substance has also adsorbed a certain amount of valuable metal ions on the other hand, causes the reduction of leach liquor ions content.2, the solid particulate in ore pulp is less, sedimentation difficulty.Due to the needs of leaching velocity and the raising of leaching yield, need to grind very little by ore particles when leaching, the particle therefore in ore pulp is often at about 1 ~ 100um.This short grained solid is difficult to rapid subsidence in the ore pulp being rich in suspended substance, and therefore cause the thickener volume carrying out ore pulp separation at present very large, floor space is huge, to adapt to the needs generated.3, a large amount of soda acid leaching agents and water is contained in ore pulp.If ore pulp is separated thorough, not only cause the waste of a large amount of leaching agent and valuable metal ions, and to cause in the slag of discharge containing a large amount of leaching agents and heavy metal ion, cause environmental pollution.
In current hydrometallurgical processes, the slurry concentrating after leaching is separated and is washed and mostly adopt thickener (CN103086548A).The principle of thickener utilizes the effect of gravity settling allow bottom slag natural subsidence to thickener, forms underflow and top leach liquor carries out solid-liquid separation.Small and the suspended substance of particle due to ore pulp as above is more, causes and utilizes merely gravity settling more difficult, thus the volume of thickener do very large, floor space also increases thereupon.In recent years in order to accelerate settling velocity, improving treatment capacity, often adopting the method (CN1621158A) adding flocculation agent.Adding of flocculation agent improves settling velocity, but make troubles also to the operation such as purification, electrolysis below.Because dissolved the flocculation agent of part in the leach liquor after clarification more or less, cause the increase of foreign matter content in leach liquor, have impact on the production of following operation and the purity of the finished product.
CN104263927A discloses the method adopting membrane pressure filter to be separated slag in ore pulp, although this kind of method has broken traditional thickener sedimentation process, this method has been made to be difficult to extensive use because of the intrinsic feature of its diaphragm filter press adopted.The shortcoming of this pressure filter is: pressure filter press filtration precision water outlet clarity is reduced, and thinner particle and suspended substance easily block and block filter cloth aperture.The barrier film of this organic material works for a long time and easy wearing and tearing can occur under soda acid soaks simultaneously, and cause pressure filter service efficiency to reduce, diaphragm replacing is frequent.
In sum, the technique that traditional slurry concentrating is separated and washing process often adopts thickener concentrated.Although it has the advantages such as treatment capacity is large, processing cost is low.But because the feature of ore pulp itself determines and adopts thickener to carry out concentrating and separating ore pulp to need huge equipment volume and huge floor space, and it is often more to carry out washing the thickener progression of needs to ore pulp; And sometimes in order to improve subsidence rate, also often add flocculation agent.So not only substantially increase the floor space of equipment, and make the solid-liquid separation process of ore pulp become complicated all the more.And concentrated supernatant liquor out is also clarified not, the slag water content settled down is high, and the amount of the valuable metal ions carried secretly increases.
Utility model content
And be the filtration belonging to high precision rank based on the ceramic membrane of aperture screening mechanism, removal for suspended substance and even slag has the ability of its uniqueness, it does not limit by the feature of ore pulp itself, do not need to add flocculation agent, filtering accuracy is high, floor space is little, can serialization, automatic operating produce, because of but a desirable separation means.And the physical strength of ceramic membrane is high, acid and alkali-resistance chemical property is good etc., and advantage makes again it can be used in harsh environmental system.
The art of this patent utilizes the screening mechanism of membrane sepn, by selecting film and the membrane module form in suitable aperture, carries out concentrating and separating and washing to ore pulp.In process, first coarse filtration is carried out to ore pulp, remove large particle, avoid producing damage to the shock of separatory membrane.Then utilize the separating film element of outer membrane type, adopt micro-cross-flow or negative pressure leaching technique and gas positive pressure squeezing process by slurry concentrating to 40 ~ 50% so that 70% concentration.Reclaim leaching liquid measure to greatest extent.Finally add washing water, when passing into air, carrying out agitator treating fully, refiltering, thus the valuable metal ions in ore pulp is fully washed out.Like this by adopting the switching of various membrane filtration pattern in process to same film, reach the object of the leach liquor in the separation ore pulp of maximum, thus improve the rate of recovery of valuable metal ions in leach liquor.Reduce the metal ion content in thickening mineral slurries, there is very high economic worth and environment protection significance.
More particularly:
An aspect of the present utility model, proposes a kind of technique of membrane separation concentration separating, washing ore pulp, comprises the steps:
1st step: the leaching ore pulp in hydrometallurgy is sent in film filter and filters, in described film filter, membrane module is installed, wherein has a membrane element at least, the inside of membrane element arranges permeate passageway, leach ore pulp from the outside of membrane element through filtration laggard enter permeate passageway, leaching ore pulp is filtered, concentrates, in permeate passageway, obtain filtered solution;
2nd step: add air pressure in the side that retains of membrane element, makes ore pulp be concentrated further;
3rd step: thin up in the ore pulp be concentrated in the 2nd step, and stirred by the mode of aeration;
4th step: filtered again by the ore pulp after diluting in the 3rd step, obtain filtrate and filter residue.
In the 1st step, when slurry concentrating to solid content is 40 ~ 50%, stop filtering.
In the 2nd step, when slurry concentrating is to solid content more than 70%, stop adding air pressure.
After the 4th step, 2nd ~ 4 steps can be repeated successively again, until the metal ion content in penetrating fluid and/or thickening mineral slurries meets the requirements.
In the 1st step and/or the 4th step, the filtration procedure of membrane module adopts the mode retaining side pressurization or per-meate side negative pressure-pumping as power.
In the 1st step and/or the 4th step, in the filtration procedure of membrane module, add backwash step; Back flushing can adopt 0.5 ~ 1wt% acid solution or alkaline solution.
Based on above-mentioned method, another aspect of the present utility model additionally provides a kind of device of membrane separation concentration separating, washing ore pulp, this device includes film filter, casing is included in film filter, settling pocket, settling pocket is arranged at the below of casing, at box house, at least one membrane element is installed, the inside of described membrane element arranges at least one permeate passageway, the outer setting of membrane element has the opening of permeate passageway, opening part is provided with seal head, the side that retains of opening and flat membrane component separates by seal head, at least one seal head is provided with membrane element and produces the mouth of a river, the below of membrane element is provided with aeration tube, casing is also provided with opening for feed and air-supply duct.
The material of membrane element is selected from metal, pottery or polymkeric substance; Membrane element is symmetric membrane or asymmetric membrane; The mean pore size scope of membrane element is 5nm ~ 5 μm.
Also being provided with at casing top can the case lid of folding.
Casing is also provided with and produces water collector, the membrane element on seal head produces the mouth of a river and produces water header in communication.
Produce water collector and be connected to clean water tank.
Product water collector is also connected with recoiling device.
Product water collector is connected with vacuum primingpump or is also connected with slush pump on casing.
The import of slush pump is connected to prefilter.
The material of seal head is polymkeric substance, is adhesively fixed between seal head and membrane element by glue.
The height of opening for feed on casing is in the middle and lower part of the vertical direction of plate film assembly, and preferably, the height of opening for feed is 1/4 ~ 1/3 place on the lower side of the vertical direction of plate film assembly.
Settling pocket is doline; The bottom of settling pocket is also provided with slag-drip opening; On the sidewall on the top of casing, be also provided with overflow port; On the inwall of the casing of the below of overflow port, weir body is also set.
Described membrane element is flat membrane element; The plane at flat membrane element place is not horizontal plane; The quantity of flat membrane element is more than two pieces.
Beneficial effect
In this patent technique, start with from the separating effect improving ore pulp, by selecting outer membrane type ceramic membrane element, adopt the mode of the micro-cross flow filter of malleation or negative pressure leaching, and be aided with gas positive pressure squeeze and filter and improve the pulp density be concentrated further, be equipped with the mode of water washing, gas stirring on this basis, reclaim in ore pulp by the metal ion leached to greatest extent.There is obvious advance, compare with membrane pressure filter with traditional thickener concentrating and separating washing process, there is following superiority:
1, the utility model provides a kind of technique of efficient ceramic membrane concentrating and separating washing ore pulp.By selecting the filtration of the ceramic membrane in high-throughout suitable aperture and concentrating, be aided with recoil and gas stirring, at the slag particle of about 10 μm and colloidal suspended substance, there is very high removal effect to particle diameter, greatly increase efficiency and the speed of concentrating and separating ore pulp.And the terminal type ceramic membrane equipment in the utility model has that volume is little, floor space is little, technique is simple, easily amplify, can run by continuous and automatic.Avoid the shortcoming that traditional thickener concentrates slowly, efficiency is low, floor space is large, bulky.
The aperture of the ceramic membrane 2, in the utility model can be selected according to the size of pulp granularity, thus avoids the blocking of ore pulp particle to ceramic fenestra.Ensure that the clarity of water outlet, the turbidity of water outlet is at about 1NTU, and compared with being about 100NTU with the delivery turbidity of traditional thickener, clarity improves greatly simultaneously.Also more much higher than the turbidity of membrane pressure filter water outlet (about 50NTU).
3, compared with diaphragm filter press, the ceramic membrane in the utility model is owing to have employed the film in suitable aperture and corresponding filtration process, and the cleaning and regeneration ratio of ceramic membrane is easier to.And due to the restriction of filtering accuracy and filter type, diaphragm filter press but easily blocks, and even occurs that filtration medium is difficult to the problem of cleaning and regeneration etc.Have impact on normally carrying out of production.Meanwhile, the difficult life of filtration medium then can cause frequently changing filtration medium, causes production cost to rise.
4, what is more important, the degree that in the utility model, gas positive pressure squeezing process makes ore pulp be concentrated is higher, and pulp density reaches 70%, and the pulp density 40 ~ 45% denser than traditional thickener is much higher.Such one side makes the amount of the leach liquor be recovered increase, and has more reclaimed valuable metal ions, makes on the other hand to adopt the washing process water yield used to be reduced.Save water resources.Be of value to environmental protection.
5, compare with diaphragm filter press with thickener, the washing process in the utility model not only water consumption reduces, and washing effect is good.Due in the utility model washing process, adopt air water agitator treating, increase metal ion to the diffusion in aqueous phase and mass transfer from slag, slag and washing water are stirred, and the concentration of metal ions carried secretly in slag the most at last drops to minimum.Both improve metal ion recovery rate, again reduce the heavy metal ion content in slag.There is obvious economy and environment benefit.
6, compared with the concentrating and separating washing process of thickener, the technique in the utility model, except process water, does not add extra medicament, needs to add flocculation agent unlike in thickener concentration process.Both reduced the expense in concentration process, saved medicament, the carrying out of next procedure and even the quality of the finished product can not have been affected because of adding of additional agent again.
Accompanying drawing explanation
Fig. 1 is setting drawing of the present utility model.
Fig. 2 is the structural representation after single flat membrane component being provided with seal head.
Fig. 3 is the structural representation of the membrane element of single hose.
Fig. 4 is the structural representation of the membrane element of multi-channel type.
Fig. 5 is the structural representation after multimodal membrane element being provided with seal head.
Fig. 6 is the front view of flat sheet membrane strainer.
Fig. 7 is the side-view of plate film assembly.
Fig. 8 is setting drawing of the present invention.
Wherein, 1, case lid; 2, sealing-ring; 3, membrane module; 4, settling pocket; 5, slag-drip opening; 6, overflow port; 7, weir body; 8, opening for feed; 9, water collector is produced; 10, bracing frame; 11, membrane element; 12, casing; 13, pickup groove; 14, membrane element produces the mouth of a river; 15, seal head; 16, permeate passageway; 17, opening; 18, air cushioning tank; 19, recoil tank; 20, clean water tank; 21, water pot; 22, vacuum primingpump; 23, water pump; 24, prefilter; 25, slush pump; 26, pulp tank; 27, aeration tube; A, source of the gas; B, ore pulp supernatant; C, slag.
Embodiment
Below by embodiment, the utility model is described in further detail.But it will be understood to those of skill in the art that the following example only for illustration of the utility model, and should not be considered as limiting scope of the present utility model.Unreceipted concrete technology or condition person in embodiment, according to the technology described by the document in this area or condition (" mineral membrane isolation technique and the application " of such as reference Xu Nan equality work, Chemical Industry Press, 2003) or carry out according to product description.Agents useful for same or the unreceipted production firm person of instrument, being can by the conventional products of commercial acquisition.
The example of described embodiment is shown in the drawings, and wherein same or similar label represents same or similar element or has element that is identical or similar functions from start to finish.Be exemplary below by the embodiment be described with reference to the drawings, be intended to for explaining the utility model, and can not be interpreted as restriction of the present utility model.In description of the present utility model, it will be appreciated that, term " " center ", " longitudinal direction ", " transverse direction ", " length ", " width ", " thickness ", " on ", D score, " front ", " afterwards ", " left side ", " right side ", " vertically ", " level ", " top ", " end " " interior ", " outward ", " clockwise ", orientation or the position relationship of the instruction such as " counterclockwise " are based on orientation shown in the drawings or position relationship, only the utility model and simplified characterization for convenience of description, instead of indicate or imply that the device of indication or element must have specific orientation, with specific azimuth configuration and operation, therefore can not be interpreted as restriction of the present utility model.
Word used herein " comprises ", " comprising ", " having " or its any other variant are intended to contain comprising of non-exclusionism.Such as, comprise technique, method, article or the equipment of listing key element and need not be limited to those key elements, but can be comprised other clearly do not list or belong to the intrinsic key element of this technique, method, article or equipment.It should be understood that when an element be mentioned " be connected " with another element time, it can directly be connected with other elements or indirectly be connected with other elements, and is inserted with element between them.
the film filter structure adopted in the utility model
The structure of the film filter adopted in the utility model is as shown in 1 ~ 7, and overall structure is as Fig. 6, and the intermediate host of strainer is casing 12, it is settling pocket 4 below it, settling pocket 4 is in doline, and the bottom of settling pocket 4 is provided with slag-drip opening 5, and the high dense slag of solid content is discharged by slag-drip opening 5 in bottom; The inside of casing 12 being provided with membrane module 3, having a membrane element 11 in membrane module 3 at least, in order to improve the filling area of device, also can be provided with multiple membrane element 11 in a casing 12, its effect is for concentrating ore pulp, filtering.
The structure of membrane element 11 is as Fig. 1, membrane element 11 role is filtered by the ore pulp of its outside, filtered solution is discharged by the permeate passageway 16 through its inside again, therefore, the inside of membrane element 11 needs to offer passage, the global shape of membrane element 11 both can be writing board shape, also can be single tube or multichannel tubular shape (as shown in Fig. 3 ~ 5).For the membrane element 11 of writing board shape, its structure as depicted in figs. 1 and 2, overall in tabular, inside arranges at least one or many permeate passageway 16, the opening 17 of permeate passageway 16 is positioned on the side of membrane element 11, and when ore pulp is after the two sides of flat membrane component 11 is subject to the effect of motivating force, the aqueous phase in ore pulp is by the filtration of membrane element 11, enter into permeate passageway 16, then flowed out by the opening 17 of permeate passageway 16; In addition, at opening 17 place, be provided with seal head 15, the retain side (or refer to the both sides external of membrane element 11) of opening 17 with membrane element 11 separates by seal head 15, the material of seal head 15 can be selected from polymer materials (rubber, silica gel, polycarbonate etc.), is fixed on opening 17, in addition by seal gum, at least one seal head 15 is provided with membrane element and produces the mouth of a river 14, membrane element produces the mouth of a river 14 and penetrating fluid can be drawn.Membrane element 11 can be symmetric membrane, also can be asymmetric membrane; When being symmetric membrane, its whole face is uniform entirety; When membrane element 11 is asymmetric membranes, its outside surface can be covered with separation membrane layer, and inside is support body layer.If adopted as shown in Fig. 3 ~ 5 during tubular membrane, its structure is also similar with the flat sheet membrane in Fig. 1 ~ 2, in membrane element 11, inside also offers permeate passageway 16, the opening 17 of permeate passageway 16 is positioned at the two ends of membrane element 11, inner at same membrane element 11, many permeate passageway 16 can be offered, when the membrane element 11 of tubular type is installed in casing, in at least one end of membrane element 11, seal head 15 will be set, the two ends of the membrane element 11 of tubular type seal by seal head 15, permeate passageway 16 and feed side side are separated, seal head 15 can be installed membrane element equally and produce the mouth of a river 14.
In a good embodiment, the structure of membrane element 11 as depicted in figs. 1 and 2, the shape of flat sheet membrane is square or rectangle, the inside of membrane element 11 offers many permeate passageway be parallel to each other 16, the opening 17 of permeate passageway 16 is positioned on the cross section at the two ends of membrane element 11, permeate passageway 16 is made to run through wherein, the section of one end wherein, seal head 15 is set, epoxy bond is adopted between seal head 15 and membrane element 11, seal head 15 is arranged a membrane element and produce the mouth of a river 14, the production water of the row of openings 17 at this end section place is all concentrated by this membrane element product mouth of a river 14 and is collected.And the other end also has a row of openings, be also sealed by seal head, separate with the side that retains of membrane element, but the seal head of this one end being installed or does not install the membrane element product mouth of a river all can.
As shown in Figure 3 and Figure 4, flat for polylith membrane element 11 is inserted side by side in casing 12, often open the distance 2 ~ 3cm between diaphragm, the seal head of the upside of membrane element 11 is fixed on the bracing frame 10 on casing 12 top, and the downside of membrane element 11 is inserted in the pickup groove 13 of casing 12 sidepiece and is fixed that (the installation fixed form of flat membrane component 11 does not have special restriction, as long as can be fixed in casing 12, also other conventional fixing part can be adopted to install), the setting angle of membrane element 11 both can with horizontal plane, also can be that plane residing for flat board and horizontal plane are kept at an angle, just can ensure that the material that flat board retains can to whereabouts, the angle α of the plane residing for flat membrane component 11 and the horizontal plane residing for bottom half is preferably 30 °≤α≤90 °.Membrane element 11, seal head 15, membrane element produce the mouth of a river 14, bracing frame 10 and pickup groove 13 and constitute the core that membrane module 3 is these strainers, filtration.Covered by case lid 1 on casing 12, form a closed casing 12, casing 12, to seal with sealing-ring 2 between case lid 1 and settling pocket 4 three part, connect with bolt.The membrane element at the top of multiple diaphragm produces the mouth of a river 14 and collects, and is connected to and produces water collector 9, the penetrating fluid on each diaphragm can be concentrated and discharge.
At the sidepiece of casing 12, be also provided with opening for feed 8, for supplying feed liquid on plate film assembly 3.The feedstock direction of opening for feed 8 is parallel to flat membrane component 11, and the height of opening for feed 8 is the inclined middle and lower part of vertical direction in casing 12 side, and the height shown in figure is 1/3 At The Height of casing upwards from bottom casing 12.On the sidewall on the top of casing 12, be also provided with overflow port 6, the discharging direction of overflow port 6 is perpendicular to plane residing for flat membrane component 11, and the effect of overflow port 6 is for discharging some feed liquids retaining side, playing the effect of certain cross-flow; In addition, preferably weir body 7 is also set in the below of overflow port 6, plays a part to remove floating matter and a small amount of backflow.
The material of flat membrane component 11 is inorganic or polymer materials, when adopting inorganic materials, can be selected from such as: titanium, stainless steel, stupalith.It is particularly preferably stupalith.As the material of the porous-film of formation ceramic separation film, suitably can select from existing known stupalith.Such as, aluminum oxide, zirconium white, magnesium oxide, silicon oxide, titanium oxide, cerium oxide, yttrium oxide can be used, the oxide materials such as barium titanate; The combined oxidation composition materials such as trichroite, mullite, forsterite, steatite, sialon, zircon, wustite; Silicon nitride, aluminum nitride and other nitride class material; The carbon compound materials such as silicon carbide; The hydroxide composition materials such as hydroxyapatite; The element such as carbon, silicon class material; Or containing their two or more inorganic composite materials etc.Natural mineral (clay, clay mineral, grog, silica sand, pottery stone, feldspar, white sand) or blast-furnace slag, flying dust etc. can also be used.Wherein, what be preferably selected from aluminum oxide, zirconium dioxide, titanium oxide, magnesium oxide, silicon oxide is one kind or two or more, the ceramic powder more preferably formed using aluminum oxide, zirconium dioxide or titanium oxide as main body.Wherein, " as main body " mentioned here represents that overall more than the 50wt% (preferred more than 75wt%, more preferably 80wt% ~ 100wt%) of ceramic powder is aluminum oxide or silicon-dioxide.Such as, in the porous material, aluminum oxide is comparatively cheap and operability is excellent.Further, the vesicular structure with the aperture being suitable for liquid separation can easily be formed, therefore, it is possible to easily manufacture the ceramic separation film with excellent liquid permeability.Further, in above-mentioned aluminum oxide, particularly preferably Alpha-alumina is used.Alpha-alumina has to be stablized in chemical and fusing point and the high characteristic of physical strength.Therefore, by using Alpha-alumina, the ceramic separation film that can utilize in wide in range purposes (such as industrial circle) can be manufactured.In addition, the mean pore size scope of membrane element 11 is 5nm ~ 5 μm, and preferably 20nm ~ 0.8 μm, is more preferably 20nm ~ 0.2 μm.
The use procedure of above-mentioned membrane module is as follows: first pending feed liquid is sent into assembly from opening for feed 8, feed liquid starts to contact with each flat membrane component 11, and upwards sluggish flow, form less cross-flow effect, solids in feed liquid retain by flat membrane component 11, under gravity, the solid-state thing that is trapped can move downward along flat membrane component 11, until from the settling pocket 4 entering bottom, and by regularly being discharged by slag-drip opening 5.The penetrating fluid of flat membrane component 11 can enter to permeate passageway 16, and is flowed out by the membrane element product mouth of a river 14 on seal head 15, and the penetrating fluid of each flat membrane component 11 can be collected by product water collector 9, and then by obtaining in membrane module producing water.In addition, owing to can contain a certain amount of scum silica frost in feed liquid, feed liquid can be discharged by overflow port 6 when moving upward, and overflow port 6 also serves the effect making the slight cross-flow of feed liquid simultaneously.
the slurry processing unit adopted in the utility model
Based on above-mentioned film filter, the structure of the slurry processing unit that the utility model adopts as shown in Figure 8, the opening for feed 8 on casing 12 is connected with slush pump 25, prefilter 24, pulp tank 26 in turn; The effect of pulp tank 26 stores ore pulp; The effect of slush pump 25 feed liquid in pulp tank 26 is sent in opening for feed 8 to filter; And the aperture of the prefilter 24 of centre is preferably less than 1mm, it plays pre-filtering effect to macrobead solid in ore pulp, and object is removed by solid filtering larger for granularity in ore pulp, causes the injury to face to avoid the particle diameter of solid too large.Ore pulp slush pump 25 after prefilter filters is got in membrane filter plant.Membrane element on the seal head 15 of membrane element 11 produces the mouth of a river 14 and is connected with product water collector 9, produces water collector 9 and is connected with clean water tank 20 again, and the product water of membrane element 11 enters into clean water tank 20 by producing water collector 9; In above-mentioned filtration procedure, have employed to provide power in the mode retaining side pressurization of film, in other a kind of form, can adopt and provide motivating force in the mode of per-meate side negative pressure-pumping, so can also be connected with vacuum primingpump 22 again on product water collector 9, by the suction function of vacuum primingpump 22, ore pulp be filtered.Membrane filtration pressure is at-0.10 ~ 0Mpa(negative pressure-pumping) or 0 ~ 0.1Mpa between (pressurization), temperature is at 10 ~ 70 DEG C.In the membrane filtration clear liquid obtained, containing the metal ion that lixiviate goes out, send in the common process such as follow-up extraction, precipitation and metal is separated.
In the process run, clear water is preferably used to recoil to membrane element 11, to eliminate the slip that membrane element 11 outside surface gathers; Can adopt and clean water tank 20 is connected with product water collector 9 by a pipeline again, this pipeline arrange charging pump the product water obtained can be realized to recoil in product water collector 9, and then enter in permeate passageway 16 to realize the back flushing to film; In some other embodiments, structure as shown in Figure 8 can be adopted, clean water tank 20 is connected with recoil tank 19, recoil tank 19 is connected with product water collector 9 again, the effect of recoil tank 9 is clear liquids of storage film strainer wherein, and recoils clear liquid in permeate passageway 16 in the middle of back flushing process; After apply pressure on recoil tank 19, the clear liquid recoil in recoil tank 19 can be made extremely to produce in water collector 9, execute stressed mode and the conventional mode such as pump, gas pressurization can be adopted to carry out, pressurizing device is connected on recoil tank 19.Pressuring method shown in figure is by adding source of the gas a in recoil tank 19, making the clear liquid in recoil tank 19 be forced out, and before source of the gas a enters in recoil tank 19, first can also be connected on surge tank 18, play the effect of buffer protection.In recoil step, backflushing medium adopts membrane module to produce water under normal circumstances, also can carry out the back flushing of chemical agent, reduce fouling membrane, improves filtration flux and efficiency, when carrying out chemistry and strengthening back flushing, can adopt 0.5 ~ 1wt% acid or alkaline solution.Acid is hydrochloric acid, nitric acid and sulfuric acid etc.; Alkali is sodium hydroxide etc.Recoil condition can be: the recoil cycle is 15 ~ 60min, and the recoil time is 10 ~ 12s.Kickback pressure is 0.15MPa.
After having carried out above-mentioned operation, the solid content of thickening mineral slurries in strainer generally can be made to reach about 40 ~ 50%, now, can by adding the mode of air pressure in casing 12, control pressure is 0.05 ~ 0.1MPa, to improve the concentration in ore pulp further, reduces the moisture in ore pulp, and then make solid content reach more than 70%, can be by being connected on source of the gas a on casing 12; Source of the gas a can be forwarded on casing 12 from surge tank 18.
After having carried out above-mentioned operation, the solid content of the ore pulp be trapped is comparatively large, wherein also containing some useful leaching of ores composition, therefore, can also add water in the side that retains of membrane element 11, and then filter, to make useful leaching composition be filtered off, improve yield.Casing 12 can also be connected with water pot 21, between water pot 21 and casing 12, the conventional components such as water pump 23, valve can also be installed.In addition, the below of the membrane element 11 in casing 12, aeration tube 27 can also be installed, the effect of aeration tube 27 is: after add water dilution again in above-mentioned thickening mineral slurries, air is blasted again by aeration tube 27, realize gas agitating, the mixing of water and thickening mineral slurries can be realized better in a limited space, and then improve the rate of recovery leaching composition.
In addition, above-mentioned filtration, thin up, this flow process of aeration agitation can circulate and repeatedly carry out, until the ion in ore pulp is washed out as much as possible, can ensure yield, and reduce metal content wherein when ore pulp is discharged, and avoid environmental pollution.The filtrate obtained can adopt conventional extraction, the precipitator method are separated metal wherein, purify.
Reference examples
By the ore pulp of certain zinc ore, the particle of ore pulp accounts for 97 ~ 98%, pH=5.2 ~ 5.4, ore pulp solid content 10% ~ 12% for being less than less than 150 μm, containing zine ion 120 ~ 130g/L in leach liquor.After squeezing into thickener with pump, add 0.3% polyacrylamide flocculating settling, the concentrating clarifying through thickener is separated, and containing solid in supernatant liquor is 0.6 ~ 1.5g/L, and in dope, solid content is 40 ~ 50%, and concentrated speed is 4.5m
3/ h, reaches 40/L containing zinc ion concentration in dense mud.Adopt plate-and-frame filter press to filter in dense mud, after filtering, pulp density only can reach 60%, then adopts water washing, and grain slag, than being 10:1, makes the zinc ion content in slag drop to 10g/L.
Embodiment 1
Same ore pulp is adopted the utility model art breading, enters in terminal type ceramic membrane filter system as shown in Figure 8, film filter is wherein the flat sheet membrane strainer as shown in Fig. 1,2,6.After filtering through the prefilter of 1mm, pump into terminal type ceramic membrane equipment through mud, filter and adopt negative pressure vacuumizing filtration, control pressure is-0.05MPa, and temperature is normal temperature.Membrane element is flat sheet membrane, and aperture is 0.2 μm.In filtration procedure, every 20min is with producing water recoil once, and kickback pressure is 0.15MPa.Every 8h adopts 0.5% sulphuric acid soln recoil once.The flux of film is at 108L/m
2more than h.The turbidity of membrane filtration clear liquid reaches 0.45NTU, the solid content of dope reaches after 40%, adopt gas positive pressure squeeze and filter, pressure is 0.05 ~ 0.1MPa, until the solid content of ore pulp reaches 70%, then add water washing, blowing air stirs, through 2 ~ 3 washings, grain slag drops to below 3g/L than for the zinc ion content in 7:1 slag.
Embodiment 2
Same ore pulp is adopted the utility model art breading, enters in terminal type ceramic membrane filter system as shown in Figure 8, film filter is wherein the flat sheet membrane strainer as shown in Fig. 1,2,6.After filtering through the prefilter of 1mm, pump into terminal type ceramic membrane equipment through mud, filter and adopt the micro-cross flow filter of malleation, control pressure is 0.05MPa, and temperature is normal temperature.Membrane element is flat sheet membrane, and aperture is 0.1 μm.In filtration procedure, every 15min is with producing water recoil once, and kickback pressure is 0.15MPa.Every 8h adopts 0.5% sulphuric acid soln recoil once.The flux of film is at 100L/m
2more than h.The turbidity of membrane filtration clear liquid reaches 0.3NTU, and the solid content of dope reaches 42%.Afterwards, adopt gas positive pressure squeeze and filter, pressure be 0.05 ~ 0.1MPa. until the solid content of ore pulp reaches 68%, then add water washing, blowing air stirs, and through 3 washings, grain slag drops to below 3g/L than for the zinc ion content in 8:1 slag.
Embodiment 3
Same ore pulp is adopted the utility model art breading, enters in terminal type ceramic membrane filter system as shown in Figure 8, film filter is wherein the flat sheet membrane strainer as shown in Fig. 1,2,6.After filtering through the prefilter of 1mm, pump into terminal type ceramic membrane equipment through mud, filter and adopt negative pressure vacuumizing filtration, control pressure is-0.07MPa, and temperature is normal temperature.Membrane element is tubular membrane, and aperture is 0.5 μm.In filtration procedure, every 40min is with producing water recoil once, and kickback pressure is 0.15MPa.Every 10h adopts 0.5% sulphuric acid soln recoil once.The flux of film is at 130L/m
2more than h.The turbidity of membrane filtration clear liquid reaches 0.5NTU, and the solid content of dope reaches 45%.Afterwards, adopt gas positive pressure squeeze and filter, pressure be 0.05 ~ 0.1MPa. until the solid content of ore pulp reaches 71%, then add water washing, blowing air stirs, and through 2 ~ 3 washings, grain slag drops to below 3g/L than for the zinc ion content in 6.5:1 slag.
Claims (7)
1. the device of a membrane separation concentration separating, washing ore pulp, it is characterized in that, film filter is included in described device, casing (12) is included in film filter, settling pocket (4), settling pocket (4) is arranged at the below of casing (12), in casing (12) inside, at least one membrane element (11) is installed, the inside of described membrane element (11) arranges at least one permeate passageway (16), the outer setting of membrane element (11) has the opening (17) of permeate passageway (16), opening (17) place is provided with seal head (15), the retain side of opening (17) with membrane element (11) separates by seal head (15), at least one seal head (15) is provided with membrane element and produces the mouth of a river (14), the below of membrane element (11) is provided with aeration tube (27), casing (12) is also provided with opening for feed (8) and air-supply duct.
2. the device of membrane separation concentration separating, washing ore pulp according to claim 1, is characterized in that: the material of membrane element (11) is selected from metal, pottery or polymkeric substance; Membrane element (11) is symmetric membrane or asymmetric membrane; The mean pore size scope of membrane element is 5nm ~ 5 μm.
3. the device of membrane separation concentration separating, washing ore pulp according to claim 1, is characterized in that: being also provided with at casing (12) top can the case lid (1) of folding; Casing (12) is also provided with and produces water collector (9), the membrane element on seal head (15) produces the mouth of a river (14) and is communicated with product water collector (9); Produce water collector (9) and be connected to clean water tank (20); Product water collector (9) is also connected with recoiling device.
4. the device of membrane separation concentration separating, washing ore pulp according to claim 1, is characterized in that: be connected with vacuum primingpump (22) or be also connected with slush pump (25) on casing (12) on product water collector (9); The import of slush pump (25) is connected to prefilter (24); The material of seal head (15) is polymkeric substance, is adhesively fixed between seal head (15) and membrane element (11) by glue.
5. the device of membrane separation concentration separating, washing ore pulp according to claim 1, is characterized in that: the height of opening for feed (8) is casing (12) 1/4 ~ 1/3 place highly of rising from casing (12) bottom upwards.
6. the device of membrane separation concentration separating, washing ore pulp according to claim 1, is characterized in that: settling pocket (4) is in doline; The bottom of settling pocket (4) is also provided with slag-drip opening (5); On the sidewall on the top of casing (12), be also provided with overflow port (6); On the inwall of the casing of the below of overflow port (6), weir body (7) is also set.
7. the device of membrane separation concentration separating, washing ore pulp according to claim 1, is characterized in that: described membrane element (11) is flat membrane element; The plane at flat membrane element place is not horizontal plane; The quantity of flat membrane element is more than two pieces.
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| CN201520827232.4U CN205099491U (en) | 2015-10-22 | 2015-10-22 | Device of concentrated separation washing ore pulp of membrane separation |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105384269A (en) * | 2015-10-22 | 2016-03-09 | 江苏久吾高科技股份有限公司 | Membrane separation technology for concentrating, separating and washing ore pulp and device thereof |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105384269A (en) * | 2015-10-22 | 2016-03-09 | 江苏久吾高科技股份有限公司 | Membrane separation technology for concentrating, separating and washing ore pulp and device thereof |
| CN105384269B (en) * | 2015-10-22 | 2018-05-04 | 江苏久吾高科技股份有限公司 | A kind of technique and device of membrane separation concentration separating, washing ore pulp |
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