CN113019712A - Flotation size mixing device based on micro-nano bubble of regulation and control interface - Google Patents
Flotation size mixing device based on micro-nano bubble of regulation and control interface Download PDFInfo
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
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- B03D1/14—Flotation machines
- B03D1/16—Flotation machines with impellers; Subaeration machines
Abstract
The invention discloses a flotation size mixing device based on interface micro-nano bubbles regulation and control, which comprises a stirring mechanism, a driving mechanism and an interface micro-nano bubble controller, wherein the interface micro-nano bubble controller comprises a first pipe body and a second pipe body, one end of the first pipe body is connected with a discharge end of the stirring mechanism, the other end of the first pipe body is communicated with the second pipe body, and the inner diameter of the second pipe body is smaller than that of the first pipe body; the driving mechanism is used for driving materials in the stirring mechanism to sequentially enter the first pipe body and the second pipe body. This size mixing device adopts the mode that the internal diameter of second body is less than first body, utilizes the reduction of internal diameter to increase the ore pulp velocity of flow, reaches the effect that steps down suddenly, through the size and the contact angle that flow rate change selectivity control mineral surface produced the micro-nano bubble of interface, and the selectivity improves the floatability of mineral to promote the hydrophobic reunion of micro-fine particle mineral, effectively improve flotation separation efficiency and reduce the medicament quantity.
Description
Technical Field
The invention belongs to the technical field of mineral processing, and particularly relates to a flotation size mixing device based on micro-nano bubbles of a regulation and control interface.
Background
Mineral resources are important material bases for human social progress and national economic development, and remain as main sources of energy and industrial raw materials for a long time in the future. Mineral processing is an important link in mineral resource utilization. Flotation is the most widely used mineral separation method, and the annual ore treatment amount is more than 20 hundred million tons. Along with the continuous development and utilization of mineral resources, the easily selected mineral resources are gradually exhausted, the characteristics of the mineral resources tend to be poor, fine and miscellaneous, and a plurality of problems are encountered in the flotation process. The micro-nano bubbles are widely applied in the flotation process due to the long existence time and the good bridge effect. Compared with the common micro-nano bubbles, the interface micro-nano bubbles have better selectivity and controllability, can preferentially nucleate and grow on the hydrophobic rough surface of the mineral, and can control the growth of the mineral.
At present, a great deal of scholars study flotation from the aspects of flotation reagents, solution properties, process equipment and the like, but the pulp conditioning link before flotation does not give enough attention, and the application of interface micro-nano bubbles is also reported. The ore pulp pretreatment has the functions of selectively improving the surface hydrophobicity of minerals, improving the adhesion efficiency of the minerals and flotation bubbles, reducing the dosage of flotation reagents, reducing environmental pollution and the like. The pretreated ore pulp has better flotation effect and is an essential link before flotation. Therefore, the slurry mixing device based on selective modification of mineral surface properties by regulating and controlling the micro-nano bubbles on the interface is provided, and has profound significance for effectively improving mineral flotation efficiency, reducing the dosage of reagents and reducing environmental pollution.
Disclosure of Invention
Aiming at the problems, the invention aims to provide a flotation pulp mixing device based on interface micro-nano bubbles regulation and control, wherein the pipe diameter, the length, the pulp flow rate and the like of each section of a micro-interface micro-nano bubble controller in the flotation pulp mixing device are based on a growth model of the micro-nano bubbles provided by the invention, and the optimal parameters are selected according to the actual situation, so that the optimization of mineral interface hydrophobicity difference is realized, the micro-fine mineral is subjected to hydrophobic agglomeration, and the aims of improving the flotation separation efficiency and reducing the medicament consumption are fulfilled.
The purpose of the invention is obtained by the following technical scheme:
a flotation size mixing device based on regulation and control of interface micro-nano bubbles comprises a stirring mechanism, a driving mechanism and an interface micro-nano bubble controller, wherein the interface micro-nano bubble controller comprises a first pipe body and a second pipe body, one end of the first pipe body is connected with a discharge end of the stirring mechanism, the other end of the first pipe body is communicated with the second pipe body, and the inner diameter of the second pipe body is smaller than that of the first pipe body; the driving mechanism is used for driving materials in the stirring mechanism to sequentially enter the first pipe body and the second pipe body.
Preferably, the interface micro-nano bubble controller further comprises a third pipe body, the third pipe body is coaxially connected with the discharge end of the second pipe body, and the inner diameter of the third pipe body is larger than that of the second pipe body.
Preferably, the interface micro-nano bubble controller further comprises a first connecting pipe body arranged between the first pipe body and the second pipe body and used for communicating the first pipe body with the second pipe body, and the inner diameter of the first connecting pipe body is gradually reduced from one end of the first connecting pipe body relative to the first pipe body to the other end of the first connecting pipe body.
Preferably, the inner diameter of the larger end of the first connecting pipe body is the same as the inner diameter of the first pipe body.
Preferably, the interface micro-nano bubble controller further comprises a second connection pipe body arranged between the second pipe body and the third pipe body, and the inner diameter of the second connection pipe body is gradually increased from one end of the second connection pipe body relative to the other end of the second connection pipe body.
Preferably, the inner diameter of the smaller end of the second connecting pipe body is the same as the inner diameter of the second pipe body.
Preferably, the lengths of the first pipe body and the third pipe body are both 0.1-2 m, and the lengths of the first connecting pipe body and the second connecting pipe body are both 0.5-1 m; the ratio of the inner diameters of the first pipe body and the second pipe body is 1: 0.25-0.6, and the inner diameter of the second pipe body is 0.01-0.3 m.
Preferably, the stirring mechanism, the first pipe body, the first connecting pipe body, the second connecting pipe body and the third pipe body are detachably connected in sequence.
Preferably, the driving mechanism is arranged between the stirring mechanism and the first pipe body or at the discharge end of the third pipe body.
Compared with the prior art, the invention has the following beneficial effects and progresses:
(1) compared with the prior art, the invention provides the interface micro-nano bubble controller, and different micro-nano bubbles are generated by controlling the micro-nano bubbles to carry out size mixing. On one hand, the interface micro-nano bubble controller is arranged to enable the mineral surface in the ore pulp to form interface micro-nano bubbles, so that the ore pulp has the characteristics of high selectivity, adjustability, bridging property, low energy consumption and the like, and the hydrophobicity of the mineral surface can be changed or the micro-fine mineral is made to be hydrophobic and agglomerated, so that the mineral flotation efficiency is improved and the dosage of a medicament is reduced;
(2) because the interface micro-nano bubbles are air bubbles generated by the diffusion of the dissolved gas, the pressure reduction range of the air bubbles is between normal pressure and steam pressure, and the required pulp flow rate is lower than that of common cavitation bubbles with the pressure reduction range lower than the steam pressure, the cavitation phenomenon is not easy to occur, and the equipment is not damaged.
(3) The interface micro-nano bubble controller can be designed to be installed around the stirring barrel according to the actual field process and field, or independently installed between the stirring barrel and the flotation tank or the flotation machine in a spiral shape. The two installation modes can be detached so as to be convenient for maintenance and replacement, and the pipe diameter and the length can be changed according to different required depressurization amplitudes and different required depressurization time caused by mineral property differences so as to be applied to flotation and pulp mixing of different minerals.
Drawings
Fig. 1 is a schematic structural diagram of an embodiment of a flotation size mixing device based on interface micro-nano bubbles regulation and control in operation.
Fig. 2 is a schematic structural diagram of another embodiment of the flotation size mixing device based on interface micro-nano bubble regulation and control in operation.
Fig. 3 is a schematic structural diagram of the interface micro-nano bubble controller according to the present invention.
Figure 4 is a flow chart of pulp conditioning-flotation principle.
Fig. 5 is a schematic structural view of a conventional stirring apparatus.
Detailed Description
The principles and features of this invention are described below in conjunction with the following drawings, which are set forth by way of illustration only and are not intended to limit the scope of the invention. The invention is described in more detail in the following paragraphs by way of example with reference to the accompanying drawings. Advantages and features of the present invention will become apparent from the following description and from the claims. It is to be noted that the drawings are in a very simplified form and are all used in non-precise proportions for the purpose of facilitating and distinctly claiming the embodiments of the present invention.
As shown in fig. 1-3, this embodiment provides a flotation size mixing device based on regulation and control interface micro-nano bubble, it includes rabbling mechanism 1, actuating mechanism 3 and interface micro-nano bubble controller 2, the rabbling mechanism 1 mainly used stirs the ore pulp, so that each material homogeneous mixing in the ore pulp, actuating mechanism 3 is used for driving 1 stirring of rabbling mechanism and finishes the ore pulp and gets into interface micro-nano bubble controller 2, after the ore pulp got into interface micro-nano bubble controller 2, interface micro-nano bubble controller 2 can make in the ore pulp that the ore pulp is reported to form interface micro-nano bubble, the mineral surface property can be modified to the micro-nano bubble in interface that forms or make the hydrophobic reunion of micro-fine particle mineral, thereby improve the efficiency of mineral flotation and reduce the medicament quantity.
The stirring mechanism 1 of the present embodiment can adopt the existing conventional stirring equipment, wherein the present embodiment preferably adopts the following modes: the stirring mechanism 1 comprises an ore pulp stirring barrel 11, a transmission shaft 12, an impeller 13 and a power source 14, wherein the upper part of the ore pulp stirring barrel 11 is cylindrical, the lower part of the ore pulp stirring barrel 11 is funnel-shaped, the lower part of the stirring barrel 1 is provided with an ore inlet 111, and the upper part of the stirring barrel is provided with an ore outlet 112; an accidental discharge port 113 is formed in the lower end of the funnel-shaped structure, and the accidental discharge port 113 is used for completely discharging ore pulp in the ore pulp stirring barrel 11 during equipment maintenance or failure; the upper end of the ore pulp stirring barrel 11 is provided with a chemical adding port 114 and a water replenishing port 115 for adding chemicals and water in the pulp mixing process. One end of a transmission shaft 12 is arranged in the stirring barrel 11 and is connected with an impeller 13, the other end of the transmission shaft 12 penetrates through the ore pulp stirring barrel 11 and is connected with a power source 14, the power source 14 is preferably a motor, and the motor drives the transmission shaft 12 through a belt. The top of transmission shaft 12 is provided with bearing body 121, and bearing body 121's effect is to guarantee transmission shaft 12 rotational stability.
This embodiment micro-nano bubble controller 2 in interface includes first body 21 and second body 23, first body one end with rabbling mechanism's discharge end is connected, the other end with second body intercommunication, and actuating mechanism 3 then drives the ore pulp and gets into first body 21 and second body 23 in proper order in by rabbling mechanism 1. Wherein, this embodiment the internal diameter of first body 21 is greater than the internal diameter of second body 23, and it is through the change of second body 23 internal diameter for when the ore pulp flows into in the second body 23 by first body 21, the velocity of flow increase of ore pulp, corresponding, can step down suddenly in the ore pulp behind the ore pulp inflow second body 23, and dissolve gas diffusion and form the micro-nano bubble of interface at mineral surface in the ore pulp under the pressure reduction.
Because the velocity of flow of second body 23 is higher, and in order to reduce its velocity of flow and be convenient for accept, this embodiment the micro-nano bubble controller of interface 2 still includes a third body 25, third body 25 with the discharge end coaxial coupling of second body 23, just the internal diameter of third body 5 is greater than the internal diameter of second body, so when the ore pulp by second body 23 inflow third body 25 after, the velocity of flow of ore pulp can reduce, its impact force that can reduce the ore pulp, the collection, the storage of follow-up accommodate device and ore pulp of being convenient for. When the micro-nano bubble controller 2 is specifically arranged, it is generally preferable that the inner diameter of the first tube 21 is substantially the same as the inner diameter of the third tube 25, so as to ensure the substantial symmetry of the interface micro-nano bubble controller 2. It should be noted that, in this embodiment, the inner diameters of the first tube 21 and the third tube 25 may also be set to be different, for example, the inner diameter of the third tube 25 is larger than the inner diameter of the first tube 21, and this embodiment is not limited thereto.
In order to facilitate the smooth flow of the slurry among the first tube 21, the second tube 23 and the third tube 25 and reduce the resistance caused by the difference of the inner diameters of the first tube 21, the second tube 23 and the third tube 25, the interface micro-nano bubble controller 2 of the embodiment further includes a first connecting tube 22 disposed between the first tube 21 and the second tube 23 and used for communicating the first tube 21 with the second tube 23, and a second connecting tube 24 disposed between the second tube 23 and the third tube 25 and used for communicating the second tube 23 with the third tube 25; wherein, the internal diameter of the first connecting pipe 22 is gradually reduced from one end of the first connecting pipe to the other end of the first connecting pipe, and the internal diameter of the second connecting pipe 24 is gradually increased from one end of the second connecting pipe to the other end of the second connecting pipe, and this embodiment realizes the smooth flow of the ore pulp between the first connecting pipe 21 and the second connecting pipe 23 and between the second connecting pipe 23 and the third connecting pipe 25 through the gradual change of the internal diameters of the first connecting pipe 22 and the second connecting pipe 24, so as to reduce the problem of the excessive flow resistance caused by the sudden change of the internal diameter. More preferably, the inner diameter of the larger end of the first connecting pipe 22 is the same as the inner diameter of the first pipe 21, the inner diameter of the smaller end is the same as the inner diameter of the second pipe 23, the inner diameter of the smaller end of the second connecting pipe 24 is the same as the inner diameter of the second pipe 23, and the inner diameter of the larger end is the same as the inner diameter of the third pipe 25, so that the smooth transition of the inner diameters among the first pipe 21, the second pipe 23 and the third pipe 25 can be realized, the resistance of pulp flowing is reduced to the maximum, and the stability of pulp flowing is improved.
In this embodiment, the second pipe 23 can be placed in a straight pipe manner, preferably, a coil pipe manner (to reduce the occupied position), but in this embodiment, a coil pipe structure is adopted, see fig. 2; more preferably, the second pipe 23 is wound on the slurry stirring barrel 11, so that the space occupation ratio of the whole equipment is further reduced, and the reference of fig. 1 is provided.
The driving mechanism 3 is used for driving materials in the stirring mechanism to sequentially enter the first pipe body 21, the first connecting pipe body 22, the second pipe body 23, the second connecting pipe body 24 and the third pipe body 25, the driving mechanism is a pump, and the pump is arranged between the stirring mechanism and the first pipe body 21, and refer to fig. 1-2; besides, the pump can also be arranged at the discharge end of the third tube 25, so as to realize the material transportation in a negative pressure (pumping) mode.
Referring to fig. 4, fig. 4 is a flow chart of pulp conditioning-flotation principle, as can be seen from fig. 4, the ore to be floated is prepared into pulp, the pulp is added with a pH regulator, an inhibitor, a collector and a foaming agent and then is added into the flotation conditioning device, and the pulp passes through the interface micro-nano bubble controller 2 and then enters into a flotation cell (or flotation machine) for flotation, so as to obtain the target mineral.
Referring to fig. 5, fig. 5 is a schematic structural diagram of a conventional stirring apparatus, including a barrel 41, a mine outlet 412, a mine inlet 411, a transmission shaft 42, a bearing body 421, an impeller 43, a motor 44, and a belt 441. The ore inlet 411 is located at the lower part of the barrel body 41, the ore outlet 412 is located at the upper part of the barrel body 41, the transmission shaft 42 enters the impeller 43 arranged at one end in the barrel body 41, the motor 44 provides power for the transmission shaft 42 through the belt 441, the upper end of the barrel body 41 is provided with the bearing body 421, the transmission shaft 42 penetrates through the middle part of the bearing body 421, and the bearing body 421 enables the transmission shaft 42 to run stably. The impeller 43 is used for stirring the ore pulp in the barrel body 41; the stirred ore pulp passes through an ore outlet 412 and then enters a flotation tank (or a flotation machine) for flotation, and target minerals are obtained.
Referring to fig. 1-2, the working process of the flotation size mixing device based on the interface micro-nano bubbles regulation and control provided by the invention is as follows: the ore pulp is introduced into the ore inlet 111 and enters the ore pulp stirring barrel 11, the motor 14 is started, the motor 14 drives the transmission shaft 12 through a belt, the transmission shaft 12 drives the impeller 13 to rotate, the ore pulp is stirred, the bearing body 121 arranged at the top end of the transmission shaft 12 can ensure the stable rotation of the transmission shaft 12, and meanwhile, the upper end of the ore pulp stirring barrel 11 is provided with a chemical adding port 114 and a water replenishing port 115 for adding chemicals and water; the stirred ore pulp flows into the pump 3 from the ore outlet 112, the outlet end of the pump 3 is connected with the interface micro-nano bubble controller 2, the ore pulp sequentially passes through the first pipe body 21, the first connecting pipe body 22, the second pipe body 23, the second connecting pipe body 24 and the third pipe body 25 in the interface micro-nano bubble controller 2 and then enters a flotation tank (or a flotation machine) for flotation, because the inner diameter of the second pipe body 23 is smaller than the pipe diameter of the first pipe body 21, the flow speed of the ore pulp is increased when the ore pulp passes through the second pipe body 23 to form negative pressure, and further, a large amount of interface micro-nano bubbles caused by the diffusion of dissolved gas are selectively generated on the surface of minerals in the second pipe body 23 due to sudden pressure drop, and the micro-nano bubbles are generated preferentially to the surface of minerals with better hydrophobicity, so as to achieve the effect of selectively changing the hydrophobicity of the surface of minerals and improve the adhesion efficiency of the target minerals and the, and promotes the hydrophobic agglomeration of the fine-particle minerals. Solves the problems of low adhesion efficiency of flotation bubbles and large dosage of medicament.
The present invention will be described in further detail with reference to specific examples.
By adopting the flotation size mixing device, the size of the generated interface micro-nano bubbles is 0.1-500 mu m. The size and contact angle of the interfacial micro-nano bubbles generated on the surfaces of different minerals under the pressure drop can be observed along with the change of time by the device and the method described in patent CN 202010019381.3.
The most core part of the interface micro-nano bubble controller 2 is various parameters of the second pipe body 23, so the invention establishes the following mathematical model to obtain the flow rate, the pipe inner diameter and the length of the fluid in the second pipe body 23. As for the flow velocity, the inner diameter and the length of the other parts of the interface micro-nano bubble controller 2, which are set according to the actual field requirements, usually the length ranges of the first tube 21 and the third tube 25 are both 0.1-2 m, and the length ranges of the first connecting tube 22 and the second connecting tube 24 are both 0.5-1 m.
The inner diameter and the length of the second pipe body 23 are obtained by the following method:
(1) constructing a model to obtain micro-nano bubble generation time T and pressure difference delta P under the state that the difference between the surface areas of the interface micro-nano bubbles generated on the surfaces of different kinds of minerals is maximum;
the steps of constructing the model are as follows:
(1) establishing a primary formula of the surface area of the spherical crown-shaped bubble, the volume change rate in the bubble growth process and the volume of the spherical crown-shaped bubble:
the surface area of the spherical-crown-shaped bubble is as follows:
S＝2πRh＝2πR2(1+cosθ) (1)
the volume change rate in the bubble growth process is as follows:
wherein:
the volume of the spherical-crown-shaped bubble is as follows:
in the formula: h is the height of the spherical crown bubble, m; theta is the bubble contact angle, degree; r is the bubble radius, m; v is the volume of the micro-nano bubbles, m3(ii) a t is the bubble growth time, s; d is the diffusion coefficient of dissolved gas; rho is the gas density in the mineral surface bubbles, Kg/m3(ii) a P is the ambient pressure, N/m2(ii) a σ is the bubble-liquid interfacial tension, N/m; c∞The concentration of dissolved gas in the bubbles at infinity, Kg/m3；CsFor dissolved gas concentration, Kg/m3(ii) a τ is dimensionless time; the calculation method is shown in Popov, Y, 2005.Evaporative displacement patterns of the displacement. Phys. Rev.E 71,036313.
(2) Establishing models of different stages in the theta and R changing process of the micro-nano bubbles, wherein the different stages comprise a floating stage of constant radius growth, a transition stage of changing radius and contact angle and an expansion stage of constant contact angle growth:
the model based on diffusion theory in the floating phase of constant radius growth is obtained from equations (2) (3) (4) as follows:
according to the formulas (2), (3) and (4), a model based on diffusion theory in the transition stage of simultaneous change of the radius and the contact angle can be obtained as follows:
the model based on diffusion theory in the expansion stage for constant contact angle growth can be obtained from the formulas (2), (3) and (4) as follows:
(3) determining the change curves of the surface areas S of the interface micro-nano bubbles generated on the surfaces of the minerals at different time points T under different pressure differences delta P by combining the Henry formula and the formulas (1), (5), (6) and (7), obtaining the micro-nano bubble generation time T and the pressure difference delta P under the state of the maximum difference of the surface areas of the interface micro-nano bubbles generated on the surfaces of different types of minerals according to the change curves,
the henry formula is: cs＝KHP2，C∞＝KHP1，ΔP＝P1-P2；
In the formula: kHHenry constant, whose value is influenced by temperature and solution properties; c∞The concentration of dissolved gas in the bubbles at infinity, Kg/m3；CsFor dissolved gas concentration, Kg/m3。
(4) And (2) combining the pressure difference delta P obtained in the step (1) and the Bernoulli equation to obtain the pulp flow rate in the second pipe body 23:
in the formula:P1is the pressure of the fluid in the first tube 21, pa; p2Is the pressure of the fluid in the second tube 23, pa; v. of1Is the flow velocity, m/s, of the fluid in the first tube 21; v. of2Is the flow velocity, m/s, of the fluid in the second tube 23; rho is the fluid density, kg/m3(ii) a g is the acceleration of gravity, m/s2(ii) a Δ H is a height difference, m, of the first tube 21 and the second tube 23; and Δ P ═ P1-P2；
Pipe diameter D of second pipe 232Is determined by the following formula:
in the formula: d1Is the diameter of the first tube 21; d2Is the diameter of the second tube 23. In the formulas (8) and (9), v is expressed as1、D1The parameters are conventional pulp pipeline operating parameters and are generally set according to actual ore throughput.
(5) According to the generation time T obtained in the step (1) and the flow velocity v of the fluid in the second pipe body 232Obtaining the length of the second tubular body 23:
L＝v2T (10)
in the formula: l is the length of the second pipe body, m; t is the time, s, of the ore pulp passing through the second pipe body.
The flow velocity v of the fluid in the second tube 23 can be calculated by the above formula1Inner diameter D of tube2And a length L calculated as the ratio of the internal diameters of said first tubular body 21 and second tubular body 23 for several common minerals is 1:0.25 to 0.6, wherein the negative pressure value of the ore pulp in the second pipe body 23 is 5kPa to 101kPa, and the length of the second pipe body 23 is 5 to 60 m. In practical application, the parameters of the other parts except the second tube 23 are determined according to the situation, and then the parameters are substituted into the formula to calculate the parameters of the second tube 23.
The actual ore is composed of different minerals, interface micro-nano bubbles are preferentially generated on a hydrophobic/rough mineral surface, and the generation of the interface micro-nano bubbles further enhances the hydrophobicity of the mineral surface, so that the difference between the mineral surface properties and other mineral surface properties is opened. The flotation process is a process that mineral adheres to bubbles and floats upwards, and minerals with stronger hydrophobicity are easier to adhere to the bubbles and are easier to select. Generally, after the flotation agent acts, the target mineral has stronger hydrophobicity than the gangue mineral. According to the invention, the interface micro-nano bubble controller 2 is arranged to enable the surface of the target mineral in the ore pulp to generate the interface micro-nano bubbles, so that the hydrophobicity of the surface of the target mineral is further improved, and after the ore pulp enters the flotation machine, the target mineral is more easily adhered to the flotation bubbles, so that the flotation efficiency is improved and the dosage is reduced.
Example 1
Butyl xanthate is used as a collecting agent, lime is used as a pH regulator, water glass is used as an inhibitor, 2# oil is used as a foaming agent, and a positive flotation process is adopted to enrich lead sulfide ore. The main useful minerals in the ore are galena and a small amount of zinc blende, the lead element grade is 2.2 percent, the metal minerals comprise magnetite, pyrite and the like, and the gangue minerals are mainly silicate minerals such as quartz, calcite and the like.
The first pipe 21 has an inner radius of 0.1m, a flow velocity of 1m/s and a length of 1m, and the third pipe 25 has an inner radius of 0.1m and a pulp density of 1531kg/m3Combining the formulas (1) to (10) in the specification, the pressure of the second pipe 23 is 35kPa, the pipe inner radius is 0.031m, the pulp flow rate is 10.11m/s, the length is 21.44m, and the height difference Δ H between the first pipe 21 and the third pipe 25 is 0.8 m.
In the test, the ore pulp after grinding is added into a stirring barrel, lime is added through a medicine adding port 114 to adjust the pH value to 8, and water glass, ethyl xanthate and No. 2 oil are sequentially added and stirred for 3min, 3min and 1min respectively. Then, the ore pulp is introduced into an ore inlet 111 of the flotation size mixing device for the interface micro-nano bubbles, a motor 14 is started and drives an impeller 13 to rotate, the ore pulp is stirred, the stirred ore pulp flows out of an ore outlet 112 and passes through an interface micro-nano bubble controller 2 connected with an ore pulp delivery pump 3, and in the experiment, the interface micro-nano bubble controller 2 has a structure shown in fig. 3. The ore pulp flows out of the third pipe 25 and enters a flotation tank of a conventional inflatable flotation machine to start flotation, and the flotation time is 4 min. And (3) flotation to finally obtain galena concentrate and tailings, respectively drying and weighing, testing the Pb grade of the galena in the concentrate, calculating the recovery rate of the galena concentrate, and comparing the recovery rate with the processing result (as a blank experiment) of a conventional stirring and size mixing device. The experiment carried out by the invention is the same as the blank experiment except that the stirring and size mixing device before flotation is different and the dosage of the added medicament in the invention is less. The above experiment was repeated, and the grinding fineness was 60%, 70%, 80%, and 90% of-200 mesh (-0.074mm) content, respectively.
Table 1 grade, recovery and chemical dosage of galena flotation concentrate in example 1
Table 1 shows the flotation results of the conventional mixing and size mixing equipment and the flotation size mixing device of the present invention. As can be seen from Table 1, the grade and recovery rate of flotation concentrate after pulp is treated by the pulp mixing device are improved, when the fineness of grinding is 60%, the grade of Pb of the concentrate treated by the pulp mixing device is 48.75%, the recovery rate is 68.34%, and compared with the treatment of conventional pulp mixing equipment, the grade is increased by 9.55%, and the recovery rate is increased by 6.48%; when the grinding fineness is 70%, the Pb grade of the concentrate processed by the pulp mixing device is 52.82%, the recovery rate is 71.25%, and compared with the conventional pulp mixing device, the grade is increased by 8.46%, and the recovery rate is increased by 7.73%; when the grinding fineness is 80%, the Pb grade of the concentrate processed by the pulp mixing device is 58.02%, the recovery rate is 76.11%, and compared with the conventional pulp mixing processing, the grade is increased by 10.47% and the recovery rate is increased by 9.79%; when the grinding fineness is 90%, the Pb grade of the concentrate processed by the pulp mixing device is 63.40%, the recovery rate is 80.08%, and compared with the conventional pulp mixing processing, the grade is increased by 12.17%, and the recovery rate is increased by 8.17%. Therefore, after the slurry mixing device disclosed by the invention is used, the grade and the recovery rate of the galena flotation concentrate are greatly improved compared with those of the galena flotation concentrate processed by a conventional slurry mixing device, and the dosage of the medicament is reduced.
Example 2
The feldspar of the quartz sand is separated by reverse flotation by using laurylamine as a collecting agent, water glass as an inhibitor and hydrofluoric acid as a pH regulator. Useful minerals of the raw ores are quartz, and the grade is 70.12%; the gangue minerals are mainly feldspar, and trace sericite, pyrite and acute.
The first pipe 21 has an inner radius of 0.1m, a flow velocity of 0.5m/s and a length of 1m, the third pipe 25 has an inner radius of 0.1m, and the pulp density is 1122kg/m3Combining the formulas (1) to (10) in the specification, the pressure of the second pipe 23 is 35kPa, the pipe inner radius is 0.029m, the pulp flow rate is 11.56m/s, the length is 36.24m, and the height difference Delta H between the first pipe 21 and the third pipe 25 is 0.8 m.
In the test, ore pulp after ore grinding is added into a stirring barrel, hydrofluoric acid is added to adjust the pH value to 2, and water glass and dodecylamine are sequentially added and stirred for 3min respectively. Then, the ore pulp is introduced into an ore inlet 111 of the flotation size mixing device for the interface micro-nano bubbles, a motor 14 is started and drives an impeller 13 to rotate, the ore pulp is stirred, the stirred ore pulp flows out of an ore outlet 112 and passes through an interface micro-nano bubble controller 2 connected with an ore pulp delivery pump 3, and in the experiment, the interface micro-nano bubble controller 2 has a structure shown in fig. 3. The ore pulp flows out of the third pipe 25 and enters a flotation tank of a conventional inflatable flotation machine to start flotation, and the flotation time is 4.5 min. And finally, performing flotation to obtain quartz concentrate and tailings, respectively drying and weighing, testing the grade of quartz in the concentrate, calculating the recovery rate of the quartz concentrate, and comparing the recovery rate with the processing result (as a blank experiment) of a conventional stirring and size mixing device. The experiment carried out by the invention is the same as the blank experiment except that the stirring and size mixing device before flotation is different and the dosage of the added medicament in the invention is less. The above experiment was repeated, and the grinding fineness was 60%, 70%, 80%, and 90% of-200 mesh (-0.074mm) content, respectively.
Table 2 grade, recovery and chemical dosage of the quartz sand flotation concentrate of example 2
Table 2 shows the flotation results of the conventional slurry mixing equipment and the flotation slurry mixing device of the present invention. As can be seen from Table 2, the ore pulp treated by the pulp mixing device of the invention has improved flotation concentrate grade and recovery rate. When the grinding fineness is 60 percent, the flotation concentrate SiO treated by the pulp mixing device of the invention2The grade is 91.77%, the recovery rate is 80.70%, compared with the conventional stirring and size mixing device, the grade is increased by 8.71%, and the recovery rate is increased by 6.29%; when the grinding fineness is 70%, the concentrate SiO treated by the pulp mixing device of the invention2The grade is 98.83 percent, the recovery rate is 84.09 percent, and compared with the treatment of a conventional size mixing device, the grade is improved by 9.70 percent, and the recovery rate is improved by 4.93 percent; when the grinding fineness is 80%, the concentrate SiO treated by the pulp mixing device of the invention2The grade is 99.63%, the recovery rate is 77.58%, compared with the conventional size mixing treatment, the grade is increased by 6.08%, and the recovery rate is increased by 6.85%; when the grinding fineness is 90%, the concentrate SiO treated by the pulp mixing device of the invention2The grade is 99.38%, the recovery rate is 68.92%, compared with the conventional size mixing treatment, the grade is increased by 1.58%, and the recovery rate is increased by 4.42%. Therefore, after the slurry mixing device disclosed by the invention is used, the grade and the recovery rate of quartz sand flotation concentrate are greatly improved compared with those of quartz sand flotation concentrate processed by a conventional slurry mixing device, and the dosage of a medicament is reduced.
Example 3
The method comprises the steps of separating quartz in hematite through reverse flotation by using laurylamine as a collecting agent, starch as an inhibitor and sodium hydroxide as a pH regulator. The useful mineral of the raw ore is hematite, the TFe content is 30.42%, and the iron mineral content is 43.46%; the gangue minerals are mainly quartz, and secondly pyroxene, hornblende, mica, clay minerals, and the like.
The first pipe body 21 has an inner radius of 0.1m, a flow velocity of 1m/s and a length of 1m, and the third pipe body 25 has an inner radius of0.1m, density of 1316kg/m3Combining the equations (1) to (10) in the specification, the pressure of the second pipe 23 is 30kPa, the pipe inner radius is 0.030m, the pulp flow rate is 11.13m/s, the length is 27.83m, and the height difference Δ H between the first pipe 21 and the third pipe 25 is 0.8 m.
In the test, the ore pulp after ore grinding is added into a stirring barrel, then sodium hydroxide is added to adjust the pH value to be alkalescent, and then starch and dodecylamine are added to be respectively stirred for 3 min; then, the ore pulp is introduced into an ore inlet 111 of the flotation pulp mixing device based on interface micro-nano bubble regulation and control, a motor 14 is started and drives an impeller 13 to rotate, the ore pulp is stirred, the stirred ore pulp flows out of an ore outlet 112 and passes through an interface micro-nano bubble controller 2 connected with an ore pulp delivery pump 3, and in the experiment, the interface micro-nano bubble controller 2 has a structure shown in fig. 3. The ore pulp flows out of the third pipe 25 and enters a flotation tank of a conventional inflatable flotation machine to start flotation, and the flotation time is 5 min. And finally obtaining hematite concentrate and tailings by flotation, respectively drying and weighing, testing the grade of hematite in the concentrate, calculating the recovery rate, and comparing the recovery rate with the processing result (as a blank experiment) of a conventional stirring and size mixing device. The experiment carried out by the invention is the same as the blank experiment except that the stirring and size mixing device before flotation is different and the dosage of the added medicament in the invention is less. The above experiment was repeated, and the grinding fineness was 60%, 70%, 80%, and 90% of-200 mesh (-0.074mm) content, respectively.
Table 3 grade, recovery and dose of hematite flotation concentrate in example 3
Table 3 shows the flotation results of the conventional mixing and size mixing equipment and the flotation size mixing device of the present invention. As can be seen from Table 3, the ore pulp treated by the pulp mixing device of the invention has improved flotation concentrate grade and recovery rate. When the grinding fineness is 60%, the concentrate Fe grade processed by the stirring and pulp mixing equipment is 54.80%, the recovery rate is 75.12%, and compared with the conventional pulp mixing device, the grade is increased by 7.58% and the recovery rate is increased by 6.72%; when the grinding fineness is 70%, the grade of the concentrate Fe treated by the stirring and pulp mixing equipment is 61.83%, the recovery rate is 81.42%, and compared with the treatment of a conventional pulp mixing device, the grade is increased by 9.80%, and the recovery rate is increased by 6.98%; when the grinding fineness is 80%, the concentrate Fe grade processed by the stirring and pulp mixing equipment is 68.93%, the recovery rate is 87.30%, and compared with the conventional pulp mixing device, the grade is increased by 9.28%, and the recovery rate is increased by 11.02%; when the grinding fineness is 90%, the concentrate processed by the stirring and pulp mixing equipment has the Fe grade of 66.60% and the recovery rate of 84.52%, and compared with the conventional pulp mixing device, the grade is increased by 8.28% and the recovery rate is increased by 12.37%. Therefore, after the slurry mixing device disclosed by the invention is used, the grade and the recovery rate of hematite flotation concentrate are greatly improved compared with those of hematite flotation concentrate processed by a conventional slurry mixing device, and the dosage of a medicament is reduced.
Example 4
The method adopts kerosene as a collecting agent and octanol as a foaming agent to separate quartz and kaolinite in a coal mine by direct flotation. The useful mineral of the raw ore is coal; gangue minerals are mainly quartz and kaolinite.
The inner radius of the first pipe body 21 is 0.1m, the flow velocity is 1m/s, the length is 1m, the inner radius of the third pipe body 25 is 0.1m, and the pulp density is 1053kg/m3Combining the formulas (1) to (10) in the specification, the pressure of the second pipe 23 is 60kPa, the pipe inner radius is 0.032m, the pulp flow velocity is 9.69m/s, the length is 19.07m, and the height difference Delta H between the first pipe 21 and the third pipe 25 is 0.8 m.
In the experiment, ore pulp after ore grinding is added into a stirring barrel, then kerosene and octanol are respectively stirred for 3min, then the ore pulp is introduced into an ore inlet 111 of the flotation size mixing device based on interface micro-nano bubbles regulation and control, a motor 14 is started and drives an impeller 13 to rotate, the ore pulp is stirred, the stirred ore pulp flows out of an ore outlet 112 and passes through an interface micro-nano bubble controller 2 connected with an ore pulp delivery pump 3, and in the experiment, the interface micro-nano bubble controller 2 is in a structure shown in fig. 3. The ore pulp flows out of the third pipe 25 and enters a flotation tank of a conventional inflatable flotation machine to start flotation, and the flotation time is 3 min. And finally obtaining hematite concentrate and tailings by flotation, respectively drying and weighing the hematite concentrate and the tailings, testing the grade of coal in the concentrate, calculating the recovery rate of the hematite concentrate, and comparing the recovery rate with the processing result (as a blank experiment) of a conventional stirring and size mixing device. The experiment carried out by the invention is the same as the blank experiment except that the stirring and size mixing device before flotation is different and the dosage of the added medicament in the invention is less. The above experiment was repeated, and the grinding fineness was 60%, 70%, 80%, and 90% of-200 mesh (-0.074mm) content, respectively.
Table 4 yield, ash content and dosage of chemicals for coal mine flotation concentrate in example 4
Table 4 shows the flotation results of the conventional mixing and size mixing equipment and the flotation size mixing device of the present invention. As can be seen from Table 4, the ore pulp treated by the pulp mixing device of the invention has improved flotation concentrate grade and recovery rate. When the grinding fineness is 60%, the yield of the treatment by the stirring and pulp mixing equipment is 78.10%, the ash content is 7.66%, and compared with the treatment by a conventional pulp mixing device, the yield is increased by 8.80%, and the ash content is reduced by 2.86%; when the grinding fineness is 70%, the yield of the slurry treated by the stirring and mixing equipment is 80.04%, the ash content is 6.25%, and compared with the conventional slurry mixing device, the yield is increased by 7.52% and the ash content is reduced by 3.30%; when the grinding fineness is 80%, the yield of the treatment by the stirring and pulp mixing equipment is 86.22%, the ash content is 5.63%, and compared with the treatment by a conventional pulp mixing device, the yield is increased by 8.36%, and the ash content is reduced by 3.57%; when the grinding fineness is 90%, the yield of the treatment by the stirring and pulp mixing equipment is 82.67%, the ash content is 6.75%, and compared with the treatment by a conventional pulp mixing device, the yield is increased by 6.82%, and the ash content is reduced by 2.67%; therefore, the ash content and the yield of the coal mine flotation concentrate are greatly reduced and improved compared with the ash content and the yield of the coal mine flotation concentrate processed by the conventional size mixing device, and the dosage of the medicament is reduced.
The above embodiments are preferred embodiments of the present invention, but the embodiments of the present invention are not limited to the above embodiments, and any other changes, modifications, substitutions, combinations, and simplifications which do not depart from the spirit and principle of the present invention should be regarded as equivalent replacements, and still fall within the protection scope of the technical solution of the present invention.
Claims (9)
1. A flotation size mixing device based on regulation and control of interface micro-nano bubbles is characterized by comprising a stirring mechanism, a driving mechanism and an interface micro-nano bubble controller, wherein the interface micro-nano bubble controller comprises a first pipe body and a second pipe body, one end of the first pipe body is connected with a discharge end of the stirring mechanism, the other end of the first pipe body is communicated with the second pipe body, and the inner diameter of the second pipe body is smaller than that of the first pipe body; the driving mechanism is used for driving materials in the stirring mechanism to sequentially enter the first pipe body and the second pipe body.
2. The flotation size mixing device based on the regulation and control of the interface micro-nano bubbles is characterized in that the interface micro-nano bubble controller further comprises a third pipe body, the third pipe body is coaxially connected with the discharge end of the second pipe body, and the inner diameter of the third pipe body is larger than that of the second pipe body.
3. The flotation size mixing device based on the regulation and control of the interface micro-nano bubbles is characterized in that the interface micro-nano bubble controller further comprises a first connecting pipe body which is arranged between the first pipe body and the second pipe body and used for communicating the first pipe body and the second pipe body, and the inner diameter of the first connecting pipe body is gradually reduced from one end, opposite to the first pipe body, of the first connecting pipe body to the other end of the first connecting pipe body.
4. The flotation size mixing device based on the micro-nano bubbles with the regulated interfaces as claimed in claim 3, wherein the inner diameter of the larger end of the first connecting pipe body is the same as the inner diameter of the first pipe body.
5. The flotation size mixing device based on the regulation and control of the interface micro-nano bubbles is characterized in that the interface micro-nano bubble controller further comprises a second connecting pipe body arranged between the second pipe body and the third pipe body, and the inner diameter of the second connecting pipe body is gradually increased from one end, opposite to the second pipe body, of the second connecting pipe body to the other end of the second connecting pipe body.
6. The flotation size mixing device based on the micro-nano bubbles at the regulation and control interface of claim 5 is characterized in that the inner diameter of the smaller end of the second connecting pipe body is the same as the inner diameter of the second pipe body.
7. The flotation size mixing device based on the micro-nano bubbles with the regulated interfaces as claimed in claim 5, wherein the lengths of the first pipe body and the third pipe body are both 0.1-2 m, and the lengths of the first connecting pipe body and the second connecting pipe body are both 0.5-1 m; the ratio of the inner diameters of the first pipe body and the second pipe body is 1: 0.25-0.6, and the inner diameter of the second pipe body is 0.01-0.3 m.
8. The flotation size mixing device based on micro-nano bubbles at regulation and control interface of claim 5, wherein the stirring mechanism, the first pipe body, the first connecting pipe body, the second connecting pipe body and the third pipe body are detachably connected in sequence.
9. The flotation size mixing device based on the micro-nano bubbles of the regulation and control interface of claim 2, wherein the driving mechanism is arranged between the stirring mechanism and the first pipe body or at the discharge end of the third pipe body.
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Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| SU806129A1 (en) * | 1977-06-01 | 1981-02-23 | Всесоюзный Научно-Исследовательскийи Проектный Институт Золотодобывающейпромышленности "Вниипрозолото" | Column-type flotation machine |
| SU1297921A1 (en) * | 1985-10-22 | 1987-03-23 | Грузинский политехнический институт им.В.И.Ленина | Pneumatic flotation column machine |
| CN101306398A (en) * | 2007-05-15 | 2008-11-19 | 上海大屯能源股份有限公司 | Microbubble swirl separation method and divice |
| CN101757987A (en) * | 2010-01-12 | 2010-06-30 | 中南大学 | Flotation column |
| CN206454796U (en) * | 2017-01-09 | 2017-09-01 | 中国矿业大学(北京) | A kind of laboratory coal slime pressure dissolved air floatation device |
| CN108380397A (en) * | 2018-05-17 | 2018-08-10 | 中国矿业大学 | A kind of recovery method of low concentration calcite type containing mica fluorite tailing |
-
2021
- 2021-03-01 CN CN202110224230.6A patent/CN113019712A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| SU806129A1 (en) * | 1977-06-01 | 1981-02-23 | Всесоюзный Научно-Исследовательскийи Проектный Институт Золотодобывающейпромышленности "Вниипрозолото" | Column-type flotation machine |
| SU1297921A1 (en) * | 1985-10-22 | 1987-03-23 | Грузинский политехнический институт им.В.И.Ленина | Pneumatic flotation column machine |
| CN101306398A (en) * | 2007-05-15 | 2008-11-19 | 上海大屯能源股份有限公司 | Microbubble swirl separation method and divice |
| CN101757987A (en) * | 2010-01-12 | 2010-06-30 | 中南大学 | Flotation column |
| CN206454796U (en) * | 2017-01-09 | 2017-09-01 | 中国矿业大学(北京) | A kind of laboratory coal slime pressure dissolved air floatation device |
| CN108380397A (en) * | 2018-05-17 | 2018-08-10 | 中国矿业大学 | A kind of recovery method of low concentration calcite type containing mica fluorite tailing |
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