CN105384269B - A kind of technique and device of membrane separation concentration separating, washing ore pulp - Google Patents
A kind of technique and device of membrane separation concentration separating, washing ore pulp Download PDFInfo
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- CN105384269B CN105384269B CN201510695982.5A CN201510695982A CN105384269B CN 105384269 B CN105384269 B CN 105384269B CN 201510695982 A CN201510695982 A CN 201510695982A CN 105384269 B CN105384269 B CN 105384269B
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Abstract
The present invention relates to a kind of technique and device of membrane separation concentration separating, washing ore pulp, belong to field of hydrometallurgy.Technique includes：By pending ore pulp after prefilter filters, squeezed into pump in terminal type separation membrane filter system, using the micro- cross-flow of positive pressure or negative pressure leaching, the clear liquid after filtering discharge terminal type after clear liquid manifold collects and separates film device, can direct reuse to next procedure；High-concentration ore slurry after filtering is squeezed by gas positive pressure again, further improves the concentration of ore pulp；The ore pulp pressed dry is added and is followed by stirring and washing with gas after water, the step of ore pulp after washing carries out last time circulation, until the valuable metal ions content in ore pulp is reduced to the degree that can be discharged.Terminal type separation membrane filtration system in the present invention is core, pass through the micro- cross-flow filtration of positive pressure or negative pressure leaching, it is ensured that the separated continuous production of slurry concentrating, passes through gas positive pressure squeezing and aqueous vapor agitator treating, the rate of recovery of the metal ion in ore pulp is improved, reduces investment and operating cost.
Description
Technical field
The present invention relates to a kind of technique of ceramic membrane concentrating and separating washing ore pulp, relates in particular to one kind and uses terminal type
Ceramic membrane filter equipment concentrating and separating washs the technique of ore pulp, belongs to field of hydrometallurgy.
Background technology
In hydrometallurgy process, after ore pulp acid adding alkali medicament leaches, the separation of solid and liquid between leachate and slag need to be carried out,
To obtain the leachate containing valuable metal ions, next process deep processing is carried out.This ore pulp has following feature：1、
Solid content is bigger in ore pulp, reaches 10~15%.Solid content is not in addition to occurring the slag of Leach reaction, also containing more
The suspended solids generated by Leach reaction.On the one hand this suspended solids add the density and viscosity of ore pulp, hinder
The sedimentation of slag；The porosity and looseness of another aspect suspended matter has also adsorbed a certain amount of valuable metal ions, causes leaching
The reduction of liquid ions content.2nd, the solid particle in ore pulp is smaller, and sedimentation is difficult.Due to the needs and leaching rate of leaching velocity
Raising, it is necessary to ore particles be ground to obtain very little when leaching, therefore the particle in ore pulp is often in 1~100um or so.It is this small
The solid of particle is difficult to rapid subsidence in the ore pulp rich in suspended matter, therefore causes and carry out the separated concentrator of ore pulp at present
Sufficiently bulky, floor space is huge, to adapt to the needs of generation.3rd, substantial amounts of soda acid leaching agent and water are contained in ore pulp.If
Ore pulp separation is not thorough, and not only causes the waste of a large amount of leaching agents and valuable metal ions, but also is caused in the slag of discharge
Containing substantial amounts of leaching agent and heavy metal ion, environmental pollution is caused.
Separated at present in hydrometallurgical processes for the slurry concentrating after leaching and washing uses concentrator mostly
（CN103086548A）.The principle of concentrator is to allow slag natural subsidence to dense motor spindle, shape using the effect of gravitational settling
Separation of solid and liquid is carried out into underflow and top leachate.Since the particle of ore pulp as described above is small and the more original of suspended matter
Cause, cause merely using gravitational settling it is relatively difficult so that the volume of concentrator is made big, floor space also increases therewith
Greatly.In recent years in order to accelerate sinking speed, treating capacity is improved, often using the method for adding flocculant（CN1621158A）.Flocculation
The addition of agent is to improve sinking speed, but is also made troubles to processes such as following purification, electrolysis.Because the leaching after clarification
Go out in liquid more or less to have dissolved the flocculant of part, cause the increase of impurity content in leachate, have impact on following work
The production of sequence and the purity of final products.
CN104263927A discloses the method that slag in ore pulp is separated using membrane pressure filter, although such a method is beaten
Broken traditional concentrator sedimentation process, but because its diaphragm filter press used it is intrinsic the characteristics of and make it that this method is difficult
With large-scale use.The shortcomings that this filter press is：The press filtration precision of filter press causes the reduction of water outlet clarity, and thinner
Particle and suspended matter easily block and block filter cloth aperture.At the same time this organic material membrane for a long time soda acid immersion under work
Work can occur easy to wear, cause the reduction of filter press service efficiency, diaphragm replacing is frequent.
In conclusion traditional slurry concentrating separation and washing process are often using the technique of concentrator concentration.Although it
There is treating capacity is big, processing cost is low etc..But because the characteristics of ore pulp itself determines carries out concentration point using concentrator
Huge equipment volume and huge floor space are needed from ore pulp, and the concentrator series that washing needs are carried out to ore pulp is past
Toward more；And sometimes for the rate of settling is improved, also tend to addition flocculant.So not only substantially increase accounting for for equipment
Ground area, and cause the solid-liquid separation process of ore pulp to become complicated all the more.And the supernatant of concentration out is also not enough clarified, and is sunk
The slag water content to lower is high, the amount increase of the valuable metal ions of entrainment.
The content of the invention
And the ceramic membrane based on aperture screening mechanism is the filtering for belonging to high-precision rank, for suspended matter or even slag
Removal has its unique ability, it is limited from the characteristics of ore pulp itself, it is not necessary to adds flocculant, filtering accuracy is high, accounts for
Ground area is small, can serialization, automatic operating production, thus be a preferable separation means.And the machinery of ceramic membrane
The advantages that intensity is high, acid and alkali-resistance chemical property is good allows it to be used in harsh environment system again.
The art of this patent utilizes the screening mechanism of UF membrane, by selecting the film and membrane module form in suitable aperture, to ore deposit
Slurry carries out concentrating and separating and washing.During, coarse filtration is carried out to ore pulp first, big particle is removed, avoids to seperation film
Hit and produce damage.Then the separating film element of outer membrane type is utilized, using micro- cross-flow or negative pressure leaching technique and gas just
Squeezing process is pressed by slurry concentrating to 40~50% or even 70% concentration.Leaching liquid measure has been recycled to greatest extent.It is eventually adding
Washings, in the case where being passed through air, carry out fully agitator treating, refilter, thus by the valuable metal in ore pulp from
Son is fully washed out.The switching of various membrane filtration patterns is used to same film so during, reaches the maximum amount of
The purpose of the leachate in ore pulp is separated, so as to improve the rate of recovery of valuable metal ions in leachate.Reduce concentration ore deposit
Metal ion content in slurry, has very high economic value and environment protection significance.
More specifically：
One aspect of the present invention, it is proposed that a kind of technique of membrane separation concentration separating, washing ore pulp, includes the following steps：
1st step：Leaching ore pulp in hydrometallurgy is sent into film filter and is filtered, is pacified in the film filter
Equipped with membrane module, wherein at least there is a membrane component, the inside of membrane component sets penetrating fluid passage, leaches ore pulp from membrane component
Channel for permeating liquid is infiltrated in outside by filtering is laggard, leaching ore pulp filtered, concentrated, filtered solution is obtained in penetrating fluid passage；
2nd step：Air pressure is added in the retention side of membrane component, ore pulp is further concentrated；
3rd step：It is diluted with water in the ore pulp being concentrated in step 2, and is stirred by way of aeration；
4th step：Ore pulp after being diluted in 3rd step is filtered again, obtains filtrate and filter residue.
In step 1, when slurry concentrating to solid content is 40~50%, filtering is stopped.
In step 2, when slurry concentrating to solid content more than 70%, stop adding air pressure.
After the 4th step, the 2nd~4 step can be repeated in again, until penetrating fluid and/or concentration ore pulp in metal from
Sub- content meets the requirements.
In the 1st step and/or the 4th step, the filter process of membrane module is taken out using the pressurization of retention side or per-meate side negative pressure
The mode of suction is as power.
In the 1st step and/or the 4th step, backwash step is added in the filter process of membrane module；Backwash can use
0.5~1wt% acid solutions or aqueous slkali.
Based on above-mentioned method, another aspect of the present invention additionally provides a kind of membrane separation concentration separating, washing ore pulp
Device, the device include film filter, and babinet, expansion chamber are included in film filter, and expansion chamber is arranged at the lower section of babinet,
At least one membrane component is installed in box house, the inside of the membrane component sets at least one penetrating fluid passage, membrane element
The outside of part is provided with the opening of penetrating fluid passage, and opening is provided with seal head, and seal head is by opening and flat membrane component
Retention side separate, be provided with least one seal head membrane component production the mouth of a river；Aeration tube is provided with below membrane component；
Feed inlet and air supply pipe are additionally provided with babinet.
Retractable case lid is additionally provided with casing top.
It is additionally provided with babinet and produces water collector, the membrane component production mouth of a river on seal head and production water header in communication.
Production water collector is connected to clean water tank.
Recoiling device is also associated with production water collector.
Self priming pump is connected with production water collector or slush pump is also associated with babinet.
Height of the feed inlet on babinet is in the middle and lower part of the vertical direction of plate film assembly, it is preferable that the height of feed inlet
Degree is on the lower side the 1/4~1/3 of the vertical direction of plate film assembly.
Beneficial effect
In this patent technique, start with from the separating effect for improving ore pulp, by selecting outer membrane type ceramic membrane element, using just
The mode of micro- cross-flow filtration or negative pressure leaching is pressed, and is aided with gas positive pressure squeeze and filter to further improve the ore pulp being concentrated dense
Degree, is equipped with water washing, the mode of Gas Stirring on this basis, recycle to greatest extent be leached in ore pulp the metal that gets off from
Son.With obvious advance, compared with traditional concentrator concentrating and separating washing process and membrane pressure filter, have as follows
Superiority：
1st, the present invention provides a kind of technique of efficient ceramic membrane concentrating and separating washing ore pulp.It is high-throughout by selecting
The filtering and concentration of the ceramic membrane in suitable aperture, are aided with recoil and Gas Stirring, to particle diameter 10 μm or so slag particle and
Colloidal suspended substance has very high removal effect, greatly increases the efficiency and speed of concentrating and separating ore pulp.And the present invention
In terminal type ceramic membrane equipment have it is small, floor space is small, technique is simple, easily amplification, can continuous and automatic run.
Avoid that the concentration of traditional concentrator is slow, efficiency is low, the shortcomings that taking up a large area, is bulky.
2nd, the aperture of the ceramic membrane in the present invention can make choice according to the size of pulp granularity, so as to avoid ore pulp
Blocking of the particle to ceramic fenestra.It ensure that the clarity of water outlet at the same time, the turbidity of water outlet is and traditional dense in 1NTU or so
The delivery turbidity of machine is compared for 100NTU or so, and clarity greatly improves.Also it is higher than the turbidity of membrane pressure filter water outlet to obtain
It is more（50NTU or so）.
3rd, compared with diaphragm filter press, film and corresponding filtering of the ceramic membrane as a result of suitable aperture in the present invention
Technique, the cleaning and regeneration of ceramic membrane are easier.And since the limitation of filtering accuracy and filter type, diaphragm filter press are easy
Block, or even the problem of filter medium is difficult to cleaning and regeneration etc. occur.It has impact on being normally carried out for production.Meanwhile filter
The difficult life of medium can then cause frequently to replace filter medium, cause production cost to rise.
4th, what is more important, gas positive pressure squeezing process causes degree higher that ore pulp is concentrated, ore pulp in the present invention
Concentration has reached 70%, and the pulp density 40~45% denser than traditional concentrator is much higher.So on the one hand so that being returned
The amount increase of the leachate of receipts, has more recycled valuable metal ions, on the other hand so that using the water used in washing process
Amount is reduced.Save water resource.It is beneficial to environmental protection.
5th, compared with concentrator and diaphragm filter press, not only water consumption is reduced the washing process in the present invention, but also is washed
Effect is good.Due in washing process of the present invention, using air water agitator treating, metal ion is increased from slag into water phase
Diffusion and mass transfer so that slag and washings stir, and the concentration of metal ions most carried secretly at last in slag drops to most
It is low.Not only metal ion recovery rate is improved, but also reduces the heavy metal ion content in slag.With obvious economy and environment
Benefit.
6th, compared with the concentrating and separating washing process of concentrator, the technique in the present invention is not added in addition to process water
Extra medicament, unlike needing to add flocculant in concentrator concentration process.Both the expense in concentration process had been reduced, had been saved
Medicament, and the progress of next procedure or even the quality of final products will not be influenced because of the addition of additional agent.
Brief description of the drawings
Fig. 1 is the structure diagram of the flat membrane component in device.
Fig. 2 is the structure diagram being provided with single flat membrane component after seal head.
Fig. 3 is the structure diagram of the membrane component of single hose.
Fig. 4 is the structure diagram of the membrane component of multi-channel type.
Fig. 5 is the structure diagram being provided with multimodal membrane component after seal head.
Fig. 6 is the front view of tablet film filter.
Fig. 7 is the side view of plate film assembly.
Fig. 8 is the device of the invention figure.
Wherein, 1, case lid；2nd, sealing ring；3rd, membrane module；4th, expansion chamber；5th, slag-drip opening；6th, overflow port；7th, weir body；8th, into
Material mouth；9th, water collector is produced；10th, supporting rack；11st, membrane component；12nd, babinet；13rd, fixing groove；14th, the membrane component production mouth of a river；15th, seal
Head；16th, penetrating fluid passage；17th, it is open；18th, air cushioning tank；19th, recoil tank；20th, clean water tank；21st, water pot；22nd, self priming pump；
23rd, water pump；24th, prefilter；25th, slush pump；26th, pulp tank；27th, aeration tube；A, source of the gas；B, ore pulp supernatant；C, slag.
Embodiment
The present invention is described in further detail below by embodiment.But those skilled in the art will manage
Solution, the following example is merely to illustrate the present invention, and should not be taken as limiting the scope of the invention.Specific skill is not specified in embodiment
Art or condition person, (such as write with reference to Xu Nan equalitys according to the described technology of document in the art or condition《Inoranic membrane point
From technology and application》, Chemical Industry Press, 2003) or carry out according to product description.Agents useful for same or instrument are not noted
Bright production firm person, being can be with conventional products that are commercially available.
The example of the embodiment is shown in the drawings, wherein same or similar label represents identical or class from beginning to end
As element or there is same or like element.The embodiments described below with reference to the accompanying drawings are exemplary, purport
For explaining the present invention, and it is not considered as limiting the invention.In the description of the present invention, it is to be understood that art
Language " " center ", " longitudinal direction ", " transverse direction ", " length ", " width ", " thickness ", " on ", " under ", "front", "rear", "left", "right", " perpendicular
Directly ", the orientation of the instruction such as " level ", " top ", " bottom " " interior ", " outer ", " clockwise ", " counterclockwise " or position relationship are based on attached
Orientation or position relationship shown in figure, are for only for ease of and describe the present invention and simplify description, rather than indicate or imply and is signified
Device or element must have specific orientation, with specific azimuth configuration and operation, therefore it is not intended that to the present invention
Limitation.
Word " comprising " used herein, "comprising", " having " or its any other variant are intended to cover non-exclusionism
Including.Technique, method, article or the equipment for e.g., including listing key element are not necessarily limited by those key elements, but can include it
He is not explicitly listed or belongs to this technique, method, article or the intrinsic key element of equipment.It should be understood that when an element
When being mentioned with another element " connection ", it can be connected directly with other elements or is indirectly connected with other elements, and
Inserted with element between them.
Film filter structure employed in the present invention
The structure of film filter employed in the present invention is as shown in 1~7, overall structure such as Fig. 6, the centre of filter
Main body is babinet 12, is below expansion chamber 4, and expansion chamber 4 is in infundibulate, and the bottom of expansion chamber 4 is provided with slag-drip opening 5, lower part
The high dense slag of solid content is discharged by slag-drip opening 5；Membrane module 3 is internally provided with babinet 12, at least one film in membrane module 3
Element 11, in order to improve the filling area of device, can also be provided with multiple membrane components 11 in a babinet 12, its effect is
For being concentrated, being filtered to ore pulp.
The structure of membrane component 11 such as Fig. 1,11 role of membrane component are to be filtered its exterior ore pulp, filtered solution
Again by being discharged through its internal penetrating fluid passage 16, therefore, the inside of membrane component 11 needs to open up passage, the entirety of membrane component 11
Shape, either writing board shape or the tubular shape of single tube or multichannel (as shown in Fig. 3~5).With
Exemplified by the membrane component 11 of writing board shape, as depicted in figs. 1 and 2, overall be in tabular to its structure, internal setting at least one or
The a plurality of penetrating fluid passage 16 of person, the opening 17 of penetrating fluid passage 16 is located on the side of membrane component 11, when ore pulp is in flat membrane
After the two sides of part 11 is driven the effect of power, the water in ore pulp enters penetrating fluid passage mutually by the filtering of membrane component 11
16, then flowed out by the opening 17 of penetrating fluid passage 16；In addition, at opening 17, seal head 15 is provided with, seal head 15 is by opening
17 separate with the retention side (or referring to the both sides external of membrane component 11) of membrane component 11, and the material of seal head 15 can be selected from poly-
Compound material（Rubber, silica gel, makrolon etc.）, it is fixed in by fluid sealant in opening 17, in addition, at least one sealing
The membrane component production mouth of a river 14 is provided with first 15, the membrane component production mouth of a river 14 can draw penetrating fluid.Membrane component 11 can be symmetrical
Film or anisotropic membrane；When being symmetric membrane, its whole film surface is uniform entirety；When membrane component 11 is anisotropic membrane
When, its outer surface can be covered with separation membrane layer, and inside is for support body layer.If used as shown in Fig. 3~5 during tubular membrane,
Its structure is also similar with the plate membrane in Fig. 1~2, and internal in membrane component 11 also to offer penetrating fluid passage 16, penetrating fluid leads to
The opening 17 in road 16 is located at the both ends of membrane component 11, inside same membrane component 11, can offer a plurality of penetrating fluid passage
16, when the membrane component 11 of tubular type is installed in babinet, seal head 15, seal head are set at least one end of membrane component 11
15 are sealed the both ends of the membrane component 11 of tubular type, penetrating fluid passage 16 is spaced with feed side side, in seal head 15
On can equally install membrane component production the mouth of a river 14.
In a preferable embodiment, as depicted in figs. 1 and 2, the shape of plate membrane is just to the structure of membrane component 11
Square or rectangle, the inside of membrane component 11 offer a plurality of penetrating fluid passage 16 being parallel to each other, and penetrating fluid passage 16 is opened
Mouth 17 makes penetrating fluid passage 16 therethrough on the section at the both ends of membrane component 11, at the section of one end wherein, if
Seal head 15 is put, is bonded between seal head 15 and membrane component 11 using epoxy resin, sets a membrane component to produce on seal head 15
The mouth of a river 14, the output water of the row of openings 17 at this end section is all produced the mouth of a river 14 and concentrated by the membrane component to be collected.And
The other end also has a row of openings, and is sealed by seal head, is spaced with the retention side of membrane component, but this one end
Installed on seal head or the membrane component production mouth of a river is not installed and all may be used.
As shown in Figure 3 and Figure 4, the flat membrane component 11 of polylith is inserted in babinet 12 side by side, between every diaphragm
2~3cm of distance, the seal head of the upside of membrane component 11 is fixed on the supporting rack 10 on 12 top of babinet, and membrane component 11
Downside is inserted in the fixing groove 13 of 12 sidepiece of babinet and is fixed（The installation fixed form of flat membrane component 11 does not have special limit
System, as long as can be fixed in babinet 12, can also use other conventional fixed components to be installed）, membrane element
The setting angle of part 11 either with horizontal plane or tablet residing for plane and horizontal plane keep certain
Angle, it is ensured that the material retained on tablet can be to whereabouts, residing for the plane and the bottom of box residing for flat membrane component 11
The angle α of horizontal plane is preferably 30 °≤α≤90 °.Membrane component 11, seal head 15, membrane component produce the mouth of a river 14, supporting rack 10 and consolidate
Determine groove 13 and constitute the core that membrane module 3 is this filter, filtration.Covered on babinet 12 by case lid 1, form one
The babinet 12 of a closing, is sealed between 4 three parts of babinet 12, case lid 1 and expansion chamber with sealing ring 2, is connected with.It is more
The membrane component production mouth of a river 14 at the top of a diaphragm is collected, and is connected to production water collector 9, can be by the penetrating fluid on each diaphragm
Concentrate discharge.
In the sidepiece of babinet 12, feed inlet 8 is additionally provided with, for supplying feed liquid on plate film assembly 3.Feed inlet 8
Feedstock direction is parallel to flat membrane component 11, the height of feed inlet 8 institute in 12 side of babinet and the inclined middle and lower part of vertical direction, figure
The height shown is at 1/3 height of babinet upward from 12 bottom of babinet.On the side wall on the top of babinet 12, it is additionally provided with
Overflow port 6, for the discharging direction of overflow port 6 perpendicular to the residing plane of flat membrane component 11, the effect of overflow port 6 is to be used to discharge
Some feed liquids of side are retained, play the role of certain cross-flow；It is further preferred to also set up weir body 7 in the lower section of overflow port 6, rise
Remove floating material and the effect to flow back on a small quantity.
The material of flat membrane component 11 is inorganic either polymeric material, when using inorganic material, Ke Yixuan
From for example：Titanium, stainless steel, ceramic material.Particularly preferably ceramic material.Material as the perforated membrane for forming ceramic separation film
Material, can suitably select from conventionally known ceramic material.It is, for example, possible to use aluminium oxide, zirconium oxide, magnesia, oxidation
The oxide materials such as silicon, titanium oxide, cerium oxide, yittrium oxide, barium titanate；Cordierite, mullite, forsterite, block are slided
The combined oxidation species material such as stone, sialon, zircon, ferrite；Silicon nitride, aluminum nitride and other nitride class material；Carbon
The carbon compound material such as SiClx；The hydroxide composition material such as hydroxyapatite；The element class material such as carbon, silicon；Or contain them
Two or more inorganic composite materials etc..It can also use natural minerals（Clay, clay mineral, grog, silica sand, pottery stone, length
Stone, white sand）Or blast-furnace slag, flying dust etc..Wherein, it is preferably selected from aluminium oxide, zirconium dioxide, titanium oxide, magnesia, silica
One kind or two or more, the ceramic powders more preferably formed using aluminium oxide, zirconium dioxide or titanium oxide as main body.Wherein,
" as main body " mentioned here represents more than the 50wt% of ceramic powders totality（It is preferred that more than 75wt%, more preferably 80wt%~
100wt%）For aluminium oxide or silica.For example, in the porous material, aluminium oxide is relatively inexpensive and operational excellent.Also,
The loose structure for having and being suitable for the separated aperture of liquid is able to easily form, therefore can easily be manufactured with excellent
The ceramic separation film of liquid permeability.Also, in above-mentioned aluminium oxide, particularly preferably using Alpha-alumina.Alpha-alumina has
The stable and characteristic of fusing point and high mechanical strength in terms of chemistry.Therefore, by using Alpha-alumina, can manufacture can be
Broad use（Such as industrial circle）The middle ceramic separation film utilized.In addition, the average pore size scope of membrane component 11 is the μ of 5nm~5
M, preferably 20nm~0.8 μm, more preferably 20nm~0.2 μm.
The use process of above-mentioned membrane module is as follows：Pending feed liquid is sent into component from feed inlet 8 first, feed liquid is opened
Beginning is in contact with each flat membrane component 11, and slowly flowing upwards, forms less cross-flow and acts on, the solid quilt in feed liquid
Flat membrane component 11 is retained, and under gravity, solid-state is trapped thing and can be moved downward along flat membrane component 11, until
From the expansion chamber 4 for entering bottom, and by periodically being discharged by slag-drip opening 5.The penetrating fluid of flat membrane component 11 can enter to infiltration
Liquid passage 16, and flowed out by the membrane component production mouth of a river 14 on seal head 15, the penetrating fluid of each flat membrane component 11 can be by production water
Collector 9 is collected, and then by obtaining production water in membrane module.Further, since can contain a certain amount of scum silica frost in feed liquid, feed liquid exists
It can be discharged upwards during movement by overflow port 6, overflow port 6 also plays the effect for making the slight cross-flow of feed liquid at the same time.
Slurry processing unit employed in the present invention
Based on above-mentioned film filter, the structure of slurry processing unit of the present invention is as shown in figure 8, in babinet 12
On feed inlet 8 on be connected with slush pump 25, prefilter 24, pulp tank 26 in turn；The effect of pulp tank 26 is storage ore pulp；
The effect of slush pump 25 is that the feed liquid in pulp tank 26 is sent into feed inlet 8 to be filtered；And middle prefilter 24
Aperture is more preferably less than 1mm, it plays pre-filtering to bulky grain solid in ore pulp, it is therefore an objective to by the solid that granularity in ore pulp is larger
It is filtered to remove, the particle diameter to avoid solid is too big and causes the injury to film surface.Ore pulp mud after prefilter filters
Stock pump 25 is got in membrane filter system.The membrane component production mouth of a river 14 on the seal head 15 of membrane component 11 is with producing 9 phase of water collector
Connection, production water collector 9 is connected with clean water tank 20 again, and the production water of membrane component 11 enters clean water tank 20 by producing water collector 9
In；It is to employ the mode pressurizeed in the retention side of film to provide power, in another form in above-mentioned filter process
In, can be using providing driving force by the way of per-meate side negative-pressure ward, then can also have been reconnected on production water collector 9 from
Sucking pump 22, is filtered ore pulp by the swabbing action of self priming pump 22.Membrane filtration pressure is in -0.10~0 Mpa（Negative pressure is taken out
Inhale）Or between 0~0.1Mpa（Pressurization）, temperature is at 10~70 DEG C.In obtained membrane filtration clear liquid, contain the metal extracted out
Ion, is sent into the common process such as follow-up extraction, precipitation and metal is separated.
During operation, it is best to use clear water recoils membrane component 11, to eliminate 11 outer surface of membrane component
The slurry of accumulation；It can use and clean water tank 20 is connected by a pipeline with production water collector 9 again, be set on this pipeline
Charging pump can be achieved to recoil obtained production water into production water collector 9, and then enter in penetrating fluid passage 16 with realization pair
The backwash of film；In some other embodiments, structure as shown in Figure 8, clean water tank 20 and recoil tank can be used
19 are connected, and recoil tank 19 is connected with production water collector 9 again, and the effect of recoil tank 9 is to store the clear liquid of film filter wherein,
And clear liquid is recoiled into penetrating fluid passage 16 among back flushing process；After application pressure on tank 19 is being recoiled, it can make
Clear liquid in recoil tank 19 recoils into production water collector 9, and the side such as conventional pump, gas pressurized can be used by applying stressed mode
Formula carries out, and pressue device is connected on recoil tank 19.Pressuring method shown in figure is by adding into recoil tank 19
Enter source of the gas a, be forced out the clear liquid in recoil tank 19, before source of the gas a enters in recoil tank 19, can also first be connected to buffering
On tank 18, play the role of buffer protection.In the step that recoils, backflushing medium, can also under normal circumstances using membrane module production water
The backwash of chemical agent is carried out, to reduce fouling membrane, improves filtration flux and efficiency, when carrying out chemistry reinforcement backwash,
0.5~1wt% acid or aqueous slkali can be used.Acid is hydrochloric acid, nitric acid and sulfuric acid etc.；Alkali is sodium hydroxide etc..Recoil condition can be with
It is：Recoil cycle is 15~60min, and recoil time is 10~12s.Kickback pressure is 0.15MPa.
After above-mentioned operation has been carried out, the solid content that can generally make to concentrate ore pulp in filter reaches 40~50%
Left and right, at this point it is possible to by way of adding air pressure into babinet 12, control pressure is 0.05~0.1MPa, so as to further
The concentration in ore pulp is improved, reduces the moisture in ore pulp, and then solid content is reached more than 70%, can be by babinet 12
On be connected on source of the gas a；Source of the gas a can be forwarded to from surge tank 18 on babinet 12.
After above-mentioned operation has been carried out, the solid content for the ore pulp being trapped is larger, wherein also useful containing some
Leaching of ores component, and hence it is also possible in the retention side Jia Shui of membrane component 11, then filtered again, so that useful leaching
Go out component to be filtered off, improve yield.Water pot 21 can also be connected with babinet 12, can also be pacified between water pot 21 and babinet 12
The conventional components such as holding water pump 23, valve.In addition, the lower section of the membrane component 11 in babinet 12, is also equipped with aeration tube 27,
The effect of aeration tube 27 is：When adding water dilution in above-mentioned concentration ore pulp and then blasting air by aeration tube 27, in fact
Existing gas agitating, can preferably realize water in a limited space and concentrate the mixing of ore pulp, and then improves and leach returning for component
Yield.
In addition, above-mentioned filtering, be diluted with water, aeration agitation this flow can be circulated and is repeated, until in ore pulp
Ion washed out as much as possible, it is ensured that yield, and reduce tenor therein when ore pulp is discharged, avoids environment
Pollution.Obtained filtrate can use conventional extraction, the precipitation method to be separated, purified to metal therein.
Reference examples
By the ore pulp of certain zinc ore, the particle of ore pulp is to account for 97~98%, pH=5.2~5.4 less than less than 150 μm, and ore pulp is solid
Content 10%~12%, 120~130g/L containing zinc ion in leachate.After squeezing into concentrator with pump, 0.3% polyacrylamide is added
Flocculating setting, separates by the concentrating clarifying of concentrator, containing solid is 0.6~1.5g/L in supernatant, solid content is in dope
40~50%, the speed of concentration is 4.5m3/ h, has reached 40/L in dense mud containing zinc ion concentration.Dense mud is used into plate and frame filter press
Filtering, pulp density is only capable of reaching 60% after filtering, and then using water washing, grain slag ratio is 10:1 so that the zinc ion in slag
Content drops to 10g/L.
Embodiment 1
Same ore pulp is handled using present invention process, into terminal type ceramic membrane filter system as shown in Figure 8,
Film filter therein is the tablet film filter as shown in Fig. 1,2,6.After being filtered by the prefilter of 1mm, through mud
Stock pump enters terminal type ceramic membrane equipment, and filtering uses negative pressure vacuumizing filtration, and control pressure is -0.05MPa, and temperature is room temperature.
Membrane component is plate membrane, and aperture is 0.2 μm.Recoiled once with production water per 20min in filter process, kickback pressure 0.15MPa.
Recoiled once using 0.5% sulfuric acid solution per 8h.The flux of film is in 108L/m2More than h.The turbidity of membrane filtration clear liquid reaches
0.45NTU, after the solid content of dope has reached 40%, using gas positive pressure squeeze and filter, pressure is 0.05~0.1MPa, directly
Solid content to ore pulp has reached 70%, and then plus water washing, blowing air stir, and by 2~3 washings, grain slag ratio is 7:1 ore deposit
Zinc ion content in slag drops to below 3g/L.
Embodiment 2
Same ore pulp is handled using present invention process, into terminal type ceramic membrane filter system as shown in Figure 8,
Film filter therein is the tablet film filter as shown in Fig. 1,2,6.After being filtered by the prefilter of 1mm, through mud
Stock pump enters terminal type ceramic membrane equipment, and filtering uses the micro- cross-flow filtration of positive pressure, and control pressure 0.05MPa, temperature is room temperature.Film
Element is plate membrane, and aperture is 0.1 μm.Recoiled once with production water per 15min in filter process, kickback pressure 0.15MPa.Often
8h is recoiled once using 0.5% sulfuric acid solution.The flux of film is in 100L/m2More than h.The turbidity of membrane filtration clear liquid reaches
0.3NTU, the solid content of dope have reached 42%.Afterwards, it is straight for 0.05~0.1MPa. using gas positive pressure squeeze and filter, pressure
Solid content to ore pulp has reached 68%, and then plus water washing, blowing air stir, and by 3 washings, grain slag ratio is 8:In 1 slag
Zinc ion content drop to below 3g/L.
Embodiment 3
Same ore pulp is handled using present invention process, into terminal type ceramic membrane filter system as shown in Figure 8,
Film filter therein is the tablet film filter as shown in Fig. 1,2,6.After being filtered by the prefilter of 1mm, through mud
Stock pump enters terminal type ceramic membrane equipment, and filtering uses negative pressure vacuumizing filtration, and control pressure is -0.07MPa, and temperature is room temperature.
Membrane component is tubular membrane, and aperture is 0.5 μm.Recoiled once with production water per 40min in filter process, kickback pressure 0.15MPa.
Recoiled once using 0.5% sulfuric acid solution per 10h.The flux of film is in 130L/m2More than h.The turbidity of membrane filtration clear liquid reaches
0.5NTU, the solid content of dope have reached 45%.Afterwards, it is straight for 0.05~0.1MPa. using gas positive pressure squeeze and filter, pressure
Solid content to ore pulp has reached 71%, and then plus water washing, blowing air stir, and by 2~3 washings, grain slag ratio is 6.5:1
Zinc ion content in slag drops to below 3g/L.
Claims (9)
1. a kind of technique of membrane separation concentration separating, washing ore pulp, it is characterised in that include the following steps：
1st step：Leaching ore pulp in hydrometallurgy is sent into film filter and is filtered, is provided with the film filter
An at least membrane component, the inside of membrane component set penetrating fluid passage, and leaching ore pulp is from the outside of membrane component after filtering
Into penetrating fluid passage, leaching ore pulp filtered, concentrated, filtered solution is obtained in penetrating fluid passage；
2nd step：Air pressure is added in the retention side of membrane component, ore pulp is further concentrated；
3rd step：It is diluted with water in the ore pulp being concentrated in step 2, and is stirred by way of aeration；
4th step：Ore pulp after being diluted in 3rd step is filtered again, obtains filtrate and filter residue；
The device that the technique uses, including：Film filter, includes babinet in film filter（12）, expansion chamber（4）, sink
Room drops（4）It is arranged at babinet（12）Lower section, in babinet（12）Inside is provided with least one membrane component（11）, the membrane element
Part（11）Inside set at least one penetrating fluid passage（16）, membrane component（11）Outside be provided with penetrating fluid passage（16）'s
Opening（17）, in opening（17）Place is provided with seal head（15）, seal head（15）By opening（17）With membrane component（11）Retention
Side separates, at least one seal head（15）On be provided with membrane component production the mouth of a river（14）；In membrane component（11）Lower section be provided with exposure
Tracheae（27）；In babinet（12）On be additionally provided with feed inlet（8）And air supply pipe；In the 1st step and/or the 4th step, the mistake of membrane module
Filtration journey is to be used as power by the way of the pressurization of retention side or per-meate side negative-pressure ward；The membrane component（11）It is tablet
Formula membrane component；Plane where flat membrane component is not horizontal plane；The quantity of flat membrane component is more than two pieces；It is flat
Membrane component is parallel between each other；Spacing between flat membrane component is 2~3cm；Plane and water where flat membrane component
Angle α scope between plane is 30 °≤α≤90 °.
2. the technique of membrane separation concentration separating, washing ore pulp according to claim 1, it is characterised in that：In step 1, when
When slurry concentrating to solid content is 40~50%, stop filtering；In step 2, when slurry concentrating to solid content more than 70%, stop
Add air pressure.
3. the technique of membrane separation concentration separating, washing ore pulp according to claim 1, it is characterised in that：After the 4th step,
The 2nd~4 step is repeated in again, until the metal ion content in penetrating fluid and/or concentration ore pulp meets the requirements.
4. the technique of membrane separation concentration separating, washing ore pulp according to claim 1, it is characterised in that：In the 1st step and/or
In 4th step, backwash step is added in the filter process of membrane module；Backwash uses 0.5~1wt% acid solutions or aqueous slkali.
A kind of 5. device of membrane separation concentration separating, washing ore pulp, it is characterised in that include film filter in the device,
Include babinet in film filter（12）, expansion chamber（4）, expansion chamber（4）It is arranged at babinet（12）Lower section, in babinet（12）It is interior
Portion is provided with least one membrane component（11）, the membrane component（11）Inside set at least one penetrating fluid passage（16）,
Membrane component（11）Outside be provided with penetrating fluid passage（16）Opening（17）, in opening（17）Place is provided with seal head（15）,
Seal head（15）By opening（17）With membrane component（11）Retention side separate, at least one seal head（15）On be provided with membrane component
Produce the mouth of a river（14）；In membrane component（11）Lower section be provided with aeration tube（27）；In babinet（12）On be additionally provided with feed inlet（8）With
Air supply pipe；The membrane component（11）It is flat membrane component；Plane where flat membrane component is not horizontal plane；It is flat
The quantity of membrane component is more than two pieces；Flat membrane component is parallel between each other；Spacing between flat membrane component is 2~
3cm；The angle α scope between plane and horizontal plane where flat membrane component is 30 °≤α≤90 °.
6. the device of membrane separation concentration separating, washing ore pulp according to claim 5, it is characterised in that：Membrane component（11）'s
Material is selected from metal, ceramics or polymer；Membrane component（11）It is symmetric membrane or anisotropic membrane；Preferably, membrane component（11）
It is anisotropic membrane, the material of supporting layer is ceramics, and surface is coated with separating layer；The material of separating layer be selected from metal, ceramics or
Polymer；The average pore size scope of membrane component is 5nm~5 μm.
7. the device of membrane separation concentration separating, washing ore pulp according to claim 6, it is characterised in that：In babinet（12）Top
Portion is additionally provided with retractable case lid（1）；In babinet（12）On be additionally provided with production water collector（9）, seal head（15）On membrane element
Part produces the mouth of a river（14）With producing water collector（9）Connection；Produce water collector（9）It is connected to clean water tank（20）；In production water collector（9）On also connect
It is connected to recoiling device.
8. the device of membrane separation concentration separating, washing ore pulp according to claim 6, it is characterised in that：In production water collector
（9）On be connected with self priming pump（22）Or in babinet（12）On be also associated with slush pump（25）；Slush pump（25）Import connection
In prefilter（24）；Seal head（15）Material be polymer, seal head（15）With membrane component（11）Between glued by glue
Connect fixation.
9. the device of membrane separation concentration separating, washing ore pulp according to claim 6, it is characterised in that：Feed inlet（8）
Babinet（12）On height in the middle and lower part of vertical direction, feed inlet（8）Height be from babinet（12）Play upward case in bottom
Body（12）At the 1/4~1/3 of height；Expansion chamber（4）In infundibulate；Expansion chamber（4）Bottom be additionally provided with slag-drip opening（5）；
Babinet（12）Top side wall on, be additionally provided with overflow port（6）；In overflow port（6）Lower section babinet inner wall on, also set
Put weir body（7）；Flat membrane component is square or rectangle；Feed inlet（8）Feedstock direction and flat membrane component residing for
Plane it is parallel.
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| CN110756512B (en) * | 2019-11-26 | 2021-09-24 | 雅安沃克林环保科技有限公司 | Micron-level high-hardness powder cleaning and separating system and method |
| CN110923447B (en) * | 2019-12-16 | 2021-07-09 | 江西思远再生资源有限公司 | Multistage countercurrent continuous washing method for superfine leaching residues |
| CN113121032B (en) * | 2019-12-31 | 2023-02-10 | 有研资源环境技术研究院(北京)有限公司 | Ship flue gas washing desulfurization wastewater treatment device and method |
| CN113415938B (en) * | 2021-07-02 | 2022-10-25 | 南京膜材料产业技术研究院有限公司 | Powder recovery method and device |
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| US8491788B2 (en) * | 2007-10-23 | 2013-07-23 | Siemens Industry, Inc. | Process for enhanced total organic carbon removal while maintaining optimum membrane filter performance |
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| CN1876569A (en) * | 2006-06-19 | 2006-12-13 | 娄进 | Production method for alumina |
| CN203291613U (en) * | 2013-04-10 | 2013-11-20 | 玉溪大红山矿业有限公司 | Ceramic filter with overflow emptying function |
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