CN111001495B - Method and device for preparing conditioning agent for mineral separation - Google Patents
Method and device for preparing conditioning agent for mineral separationInfo
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- CN111001495B CN111001495B CN201910745153.1A CN201910745153A CN111001495B CN 111001495 B CN111001495 B CN 111001495B CN 201910745153 A CN201910745153 A CN 201910745153A CN 111001495 B CN111001495 B CN 111001495B
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- mother liquor
- regulator
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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
- B03D1/00—Flotation
- B03D1/001—Flotation agents
- B03D1/018—Mixtures of inorganic and organic compounds
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/16—Evaporating by spraying
- B01D1/18—Evaporating by spraying to obtain dry solids
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
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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
- B03D2201/00—Specified effects produced by the flotation agents
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- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention discloses a method and a device for preparing a conditioning agent for mineral separation. The method comprises the following steps of S1, atomizing waste mother liquor generated in industrial production of taurine into small liquid drops, S2, gasifying solvents and low-boiling-point impurities in the small liquid drops by taking hot air as a medium, S3, collecting solids (which can be directly or indirectly used as an adjusting agent of a beneficiation reagent) formed by drying the obtained liquid drops, and collecting small-particle solids by cloth bag dust removal and water film dust removal purification of steam obtained by gasifying the solvents. According to the treatment method provided by the invention, after the waste mother liquor is subjected to spray drying, the content of impurities such as glycol, ethanolamine and the like in the solid particles is obviously reduced. The method for treating the waste mother liquor has the advantages of high speed, high efficiency and large treatment capacity, and the obtained solid particles can be applied to medicaments for mine beneficiation.
Description
Technical Field
The invention relates to a method and a device for preparing a conditioning agent for mineral separation, belonging to the field of clean production of taurine.
Background
Taurine is a specific amino acid in the organism. It has wide physiological functions, such as promoting infant brain tissue and intelligence development, enhancing cell antioxidant capacity, etc., and has been used in clinical treatment of cardiovascular diseases, diabetes, digestive tract diseases, nervous system diseases, eye diseases, etc. Due to the wide range of applications, biological extraction methods have failed to meet human requirements for taurine. More than 90% of the taurine on the market today comes from chemical synthesis methods, such as ethanolamine and ethylene oxide.
The ethanolamine method has been gradually replaced by an ethylene oxide method with high synthesis yield, low cost and short period due to low yield, high synthesis cost, long synthesis period and the like. However, by using any chemical synthesis method, corresponding byproducts are produced, for example, taurine is produced industrially by using an ethylene oxide method, and the waste mother liquor often contains not-completely extracted taurine, sodium isethionate which is not reacted, sodium sulfate which is a byproduct, ethylene glycol, ethanolamine, polymers thereof and the like.
The reaction formula for preparing taurine by an ethylene oxide method is as follows:
the side reaction formula for preparing taurine by an ethylene oxide method is as follows:
the reaction formula for preparing taurine by an ethanolamine method is as follows:
NH2CH2CH2OH+H2SO4→NH2CH2CH2OSO3H
NH2CH2CH2OSO3H+Na2SO3→NH2CH2CH2SO3H+Na2SO4
In the process of preparing taurine by an ethylene oxide method, raw material ethylene oxide can react with water to generate ethylene glycol, the ethylene glycol can generate polymerization reaction to generate polyethylene glycol, the ethylene glycol can be continuously converted into ethanolamine in ammonolysis reaction, and the ethanolamine can also generate polymerization reaction to form a polymer. In the process of preparing taurine by an ethanolamine method, raw material ethanolamine which is not reacted in the esterification reaction can be subjected to polymerization reaction to generate the polyethanol amine, and in addition, 2-amino ethanol sulfate is easy to be subjected to hydrolysis reaction in a water phase to generate the ethanolamine.
The ethanolamine method is used for preparing taurine, and the sulfonation yield is low, so that the unreacted ethanolamine can undergo polymerization reaction to generate the polyethanol amine. The taurine esters produced in the first step are susceptible to hydrolysis in the aqueous phase to produce ethanolamine and sulfuric acid.
Since the chemical synthesis method has a large capacity for preparing taurine, how to treat the waste mother liquor in the industrial production of taurine is an important subject. The use of comprehensive wastewater treatment stations is a common wastewater treatment method for pharmaceutical enterprises, for example, patent CN109761455A. The method for treating industrial wastewater has the advantages of wide application range and fine treatment steps, but the method has the advantages of multiple steps, high treatment cost and additional addition of the treatment agent. Recently, patent CN108128829A reports that a device for realizing zero emission of taurine industrial wastewater is designed, and the device carries out pretreatment and desalination on wastewater, then carries out vaporization treatment by a boiler, liquid ammonia conversion treatment, rectification treatment and the like, so as to realize zero emission of wastewater. However, the device has a complex treatment route, needs to additionally add a low-boiling-point impurity capturing agent, has high cost and long treatment period, and is not beneficial to large-scale industrial production.
Disclosure of Invention
In order to solve the problems, the invention provides a method for preparing the mineral dressing regulator by using the waste mother liquor generated in the taurine industrial production as a raw material by a spray drying method.
Specifically, the method for preparing the regulator for the ore dressing comprises the following steps:
S1, atomizing waste mother liquor generated in the industrial production of taurine into small liquid drops;
s2, gasifying and removing the solvent and impurities with boiling points lower than the temperature of the heating air in the liquid drops by taking the heating air as a medium;
S3, collecting the solid formed after the obtained liquid drops are dried.
The solid (particles) obtained in the step S3 can be used as a regulator in a reagent for ore dressing by a copper ore floatation method, and the method can further comprise operations such as purification of the regulator in order to improve the purity and quality of the regulator.
Preferably, the waste mother liquor contains sodium isethionate, sodium taurate, glycol, ethanolamine and sodium sulfate, more preferably 0.1-10% of ethanolamine, 0.1-10% of glycol, 1-15% of sodium taurate, 1-15% of sodium isethionate and 5-55% of sodium sulfate.
The process according to the invention may be carried out by conventional means in the art by feeding the spent mother liquor to a centrifugal atomizer for the above atomization, preferably by filtration treatment, for example by a filter, before the spent mother liquor enters the drying tower.
The heating mode of the hot air is preferably a heat conduction oil heat exchanger, steam heating, an electric heater or a combination of any two or three. Preferably, the air is filtered, for example by a filter, prior to being heated into the drying tower.
Preferably, the small droplets of the waste mother liquor are contacted with the hot air in a parallel flow type or a convection type.
In the parallel flow type contact mode, materials enter the drying tower from the tower top, hot air passes through the hot air distributor and uniformly enters the drying tower from the upper part of the side surface of the drying tower in a tangential mode, and the hot air contacts the materials in parallel flow, stronger wind force is needed to overcome the gravity action of the materials during discharging, so that the requirements on the performance of equipment are higher, and even if the viscosity of the materials is higher, the pipeline is not easy to block, thereby being beneficial to improving the production efficiency.
In the convection type contact mode, materials enter the drying tower from the upper part of the side face of the drying tower, hot air enters from the bottom of the drying tower uniformly in a spiral mode through the hot air distributor, the materials are in convection contact with the materials, meanwhile, the materials are sprayed out by the atomizer and fall under the action of gravity, then enter the hot air to rise in a spiral mode, the heating time of the materials is prolonged, the heat energy utilization is more sufficient, and meanwhile, the discharging is more convenient.
Preferably, the droplets obtained by the atomization in step S1 have a particle size of 1 to 1000. Mu.m, preferably 50 to 300. Mu.m. The particle size is favorable for the full contact of the liquid drops and hot air, and has the advantage of improving the drying efficiency.
Preferably, the feeding speed of the waste mother liquor is 0.1-20L/min, and preferably 1-15L/min. The feeding speed can be matched with the capacity of the drying tower and the air inlet speed, and the method has the advantages of saving energy consumption and improving production efficiency.
Preferably, the air inlet speed of the hot air is as follows:
The inlet volume flow of the hot air is 3000-20000m 3/h, preferably 4500-20000m 3/h, the induced air volume flow is 3000-25000m 3/h, preferably 6000-20000m 3/h, and the inlet volume flow is matched with the induced air volume flow, so that positive pressure or negative pressure can be formed in the drying tower system, and the drying tower has the advantages of rapidly drying liquid and rapidly transferring out dried solid.
Preferably, the rotation speed of the centrifugal atomizer is 5000-20000rpm, preferably 13000-16000rpm. The rotation speed can ensure the formation quantity of liquid drops and the required particle size, and has the advantage of improving the drying efficiency.
Preferably, the inlet air temperature of the hot air is 150-300 ℃, preferably 250-270 ℃. The air inlet temperature can ensure that the solvent and the low-boiling impurities are dried, and has the advantages of energy conservation and high efficiency.
Preferably, the warm air is exhausted at a temperature of 50-150 ℃, preferably 100-120 ℃.
Preferably, the atomization mode of the waste mother liquor is centrifugal atomization or pressure atomization.
Preferably, the pressure in the spray drying tower is either normal or negative. Wherein, the hot air reaches the drying tower through the forced draught blower, and the material draws forth the drying tower through the draught fan, and when the forced draught blower wind speed is the same with the draught fan wind speed, be ordinary pressure in the drying tower, when the forced draught blower is less than the wind speed of draught fan, the pressure in the drying tower is negative pressure.
Preferably, in step S3, cold air is introduced into the collecting end of the cyclone separator, preferably at a temperature of 0-40 ℃, and preferably the cold air is filtered by a filter. The cold air can be directly from room temperature air, and has the advantages of energy conservation and efficiency improvement.
The air purified in step S4 of the present invention may be directly discharged.
The invention also provides a solid mixture (which can be directly or indirectly used as a conditioning agent of the beneficiation reagent) or a conditioning agent for the beneficiation reagent, which is prepared by the method.
The solid (namely the regulator for the beneficiation reagent) of the waste mother liquor after spray drying contains substances such as sodium taurate, sodium isethionate, sodium sulfate and the like with specific contents, wherein an amino group-containing part in the substances can be used as a cationic capturing agent in the beneficiation reagent, an organic substance containing a sulfonic group can be used as a surfactant in the beneficiation reagent, and inorganic salts such as sodium sulfate and the like can be used as the regulator in the beneficiation reagent, so that the application effect is very remarkable.
The invention also provides a preparation system of the mineral separation regulator, which comprises a storage tank, a drying tower, a cyclone separator, a liquid atomization device, a heating air pipeline and a dust removal device for waste mother liquor in the taurine industrial production, wherein:
the storage tank of the waste mother liquor is communicated with the liquid atomization device through a pipeline, and the waste mother liquor can enter the drying tower after being atomized by the liquid atomization device and is contacted with heating air introduced by the heating air pipeline for atomization drying;
The air inlet end of the cyclone separator is communicated with the outlet of the drying tower, the air outlet end of the cyclone separator is communicated with the dust removing device, and the discharge port of the cyclone separator is connected with a storage tank of the mineral dressing regulator.
In one embodiment of the invention, the drying tower is a parallel flow drying tower, and particularly preferably a small-sized LPG parallel flow dryer, the material inlet of the drying tower and the hot air inlet of the heating air duct are both arranged at the top of the drying tower, and the bottom outlet of the drying tower is connected with the cyclone separator.
In another embodiment of the invention, the drying tower is a convection drying tower, particularly preferably a small XSG type convection drying tower, wherein the material inlet of the drying tower and the hot air inlet of the heating air pipeline are respectively arranged at the top and the bottom of the drying tower oppositely, and the top outlet of the drying tower is connected with the cyclone separator.
In the parallel flow type drying tower, as shown in fig. 1, materials are pumped to a centrifugal atomizer in the drying tower, atomized into small liquid drops, enter the drying tower from the tower top, air is filtered by a filter and then enters a heater for heating, and after entering a hot air distributor, the hot air uniformly enters the tower from the upper part of the side surface of the drying tower in a tangential mode to contact with the materials in a spiral mode.
The parallel flow type drying tower has the advantages that the material is contacted with the heat source in parallel flow, stronger gravity action of wind power customer service materials is needed during discharging, so that the requirement on equipment performance is higher, when the viscosity of the material is higher, the pipeline is not easy to be blocked, and the production efficiency is improved.
In the convection type drying tower, as shown in fig. 2, the material is pumped to a centrifugal atomizer in the drying tower, atomized into small droplets, then enters the drying tower from the upper part of the side surface of the drying tower, air is filtered by a filter and then enters a heater for heating, and after entering a hot air distributor, the hot air uniformly enters from the bottom of the drying tower in a spiral shape, and the material is contacted with hot air in a convection type.
The convection type drying tower has the advantages that the contact mode of the material and the heat source is convection, meanwhile, the material is sprayed out by the atomizer and falls under the action of gravity, then enters hot air for spiral rising, the heating time of the material is prolonged, the heat energy is utilized more fully, and meanwhile, the discharging is more convenient.
The invention also provides a method for preparing the conditioning agent for mineral separation by using the device, when in use, the air is filtered by the filter and then enters the heater for heating, and the hot air enters the hot air distributor and then uniformly enters the drying tower in a spiral shape. The material liquid is filtered by a filter and then pumped into a centrifugal atomizer in a drying tower, sprayed into mist droplets with small particle diameters, the surface of the material is contacted with hot air, water is rapidly evaporated, the material is dried into solid particles in a short time, the particles are trapped in a cyclone separator and a cloth bag dust removing device behind the tower, the particles trapped at the tail end of the cyclone separator are cooled by cold air and then packaged, and wet waste gas is further dedusted and purified by a water film dust removing device and then discharged outdoors by a fan.
The preparation system of the mineral dressing regulator has the following characteristics:
1. the drying speed is high, the surface area of liquid drops is greatly increased by centrifugal spraying of feed liquid, and 95-98% of low-boiling-point solvent and impurities can be instantaneously evaporated in high-temperature air flow, so that the drying time is only required to be several seconds.
2. The device is suitable for heat-sensitive materials, and because the liquid drops are contacted with hot air in parallel flow or convection flow, the materials cannot be overheated when the low-boiling point solvent and impurities are evaporated although the temperature of the hot air is higher.
3. The application range is wide, and a large number of materials with large physical property differences can be produced by using the method, such as polymers and resins, pigments, glass, pesticides, dairy products, fertilizers, organic compounds and the like.
4. The method for treating a large amount of wastewater in industrial production has high efficiency and low cost, and effectively reduces the waste stacking space.
The mesh size of the solid particles treated by the method of the present invention is controlled by the feed rate and the rotational speed of the centrifugal atomizer, and is 50 to 300 mesh, preferably 100 to 200 mesh.
The spray-dried solid is used as a reagent for flotation beneficiation, and experiments show that the solid obtained by drying the mother liquor at the temperature of 250-280 ℃ has good selectivity on rare metal molybdenum ores, but the concentrated mother liquor is directly used as a reagent for selecting rare metal molybdenum, so that the effect is not good.
The mineral separation principle of the invention may be that the mother liquor treated by spray drying method can partially remove low boiling point solvent, and leave high boiling point sodium isethionate with sulfonic group and taurine, while the sulfonic acid is complexed with molybdenum to form complex, floating on the surface of liquid.
The invention has the beneficial effects that:
1. The spray drying method is used for treating the waste mother liquor in the taurine industrial production, and has the advantages of high speed, high efficiency and large treatment capacity.
2. As world mineral resources are increasingly depleted, lean and complex ores are increasingly utilized, and thus the amount of ore that needs beneficiation is increasingly greater. The mineral separation can obviously improve the quality of mineral raw materials, reduce the transportation cost and the cost, and realize the comprehensive utilization of resources.
3. The mine mineral separation industry needs a large amount of medicaments and additives, and solid particles obtained by spray drying waste mother liquor can be utilized in the industry, and particularly can be used for selecting rare metal molybdenum. The green environment-friendly method for reasonably utilizing the waste mother liquor is suitable for industrial production.
Drawings
FIG. 1 is a schematic diagram of an apparatus for treating spent mother liquor in the industrial production of taurine comprising a parallel flow drying tower of the present invention;
Wherein a is a material inlet, b is a hot air inlet, c is a solid outlet;
The device comprises a parallel flow type drying tower 1, a cyclone separator 2, a cloth bag dust removing device 3 and a water film dust removing device 4.
FIG. 2 is a schematic diagram of an apparatus for treating spent mother liquor in the industrial production of taurine comprising a convection drying tower of the present invention;
Wherein a is a material inlet, b is a hot air inlet, c is a solid outlet;
the device comprises a convection type drying tower 1, a cyclone separator 2, a cloth bag dust collector 3 and a water film dust collector 4.
FIG. 3 is a schematic diagram of the beneficiation process of the present invention for beneficiating solids obtained after treating spent mother liquor in taurine industrial production.
Detailed Description
The present invention is further illustrated by the following examples, which are provided to illustrate the invention but are not intended to limit the scope thereof.
In the following examples, the solid content of the waste mother liquor was measured directly by the weightlessness method after the waste mother liquor was completely dried to obtain a dressing regulator. Adding purified water to prepare a solution with the same concentration as the solid content of the waste mother solution, determining the content of residual glycol by a chemical titration method, determining the content of taurine by a liquid chromatography method, and determining the content of ethanolamine and sodium isethionate by a nuclear magnetic internal standard method. The transmittance was measured by uv-vis spectrophotometry.
Example 1
The embodiment provides a method for treating waste mother liquor in taurine industrial production to obtain a conditioning agent for mineral separation, which comprises the following steps:
s1, delivering 1 ton of waste mother liquor obtained in taurine industrial production into a centrifugal atomizer in an XSG type convection drying tower to be atomized into small liquid drops with the particle size of 0.3-100 mu m, wherein the feeding speed of the waste mother liquor is 50L/min;
S2, enabling hot air with the temperature of 150 ℃ to enter a drying tower uniformly in a spiral mode through a hot air distributor, wherein the inlet air flow rate of the hot air is 4500m 3/h, and meanwhile, the wind power of a draught fan is adjusted to 5000m 3/h, so that negative pressure is formed in a drying chamber of a dryer;
S3, collecting solid particles formed after the liquid drops are dried in a cyclone separator behind the tower;
S4, collecting small-particle solids by the steam obtained after the solvent gasification through cloth bag dust removal, and then carrying out water film dust removal and purification.
The data obtained in this example are shown in Table 1:
TABLE 1
Example 2
The embodiment provides a method for treating waste mother liquor in the industrial production of taurine, which comprises the following steps:
s1, delivering 1 ton of waste mother liquor obtained in taurine industrial production into a centrifugal atomizer in an XSG type convection drying tower to be atomized into small liquid drops with the particle size of 0.3-100 mu m, wherein the feeding speed of the waste mother liquor is 50L/min;
S2, enabling hot air with the temperature of 200 ℃ to enter a drying tower uniformly in a spiral mode through a hot air distributor, wherein the inlet air flow rate of the hot air is 5000m 3/L, and meanwhile, the wind power of a draught fan is adjusted to 6000m 3/L, so that negative pressure is formed in a drying chamber of the dryer;
S3, collecting solid particles formed after the liquid drops are dried in a cyclone separator behind the tower;
S4, collecting small-particle solids by the steam obtained after the solvent gasification through cloth bag dust removal, and then carrying out water film dust removal and purification.
The data obtained in this example are shown in Table 2:
TABLE 2
Example 3
The embodiment provides a method for treating waste mother liquor in the industrial production of taurine, which comprises the following steps:
S1, delivering waste mother liquor obtained in industrial production of 1 ton of taurine into a centrifugal atomizer in an LPG parallel flow type drying tower to be atomized into small liquid drops with the particle size of 0.3-100 mu m, wherein the feeding speed of the waste mother liquor is 100L/min;
S2, hot air with the temperature of 260 ℃ is spirally and uniformly fed into the drying tower through a hot air distributor, wherein the inlet air flow rate of the hot air is 5000m 3/L, and meanwhile, the wind power of a draught fan is adjusted to 6000m 3/L, so that negative pressure is formed in a drying chamber of the dryer;
S3, collecting solid particles formed after the liquid drops are dried in a cyclone separator behind the tower;
S4, collecting small-particle solids by the steam obtained after the solvent gasification through cloth bag dust removal, and then carrying out water film dust removal and purification.
The data obtained in this example are shown in Table 3:
TABLE 3 Table 3
From the above examples, it can be seen that the higher the inlet air temperature, the lower the content of glycol and ethanolamine in the dried solid, and the higher the transmittance of the solution dissolved by adding purified water, but too high an inlet air temperature would have a negative effect on the equipment, for example, high requirements on the equipment, but would lead to an increase in cost, so that the inlet air temperature is preferably 260 ℃.
Example 4
The embodiment provides a preparation system of a mineral dressing regulator, as shown in fig. 1, comprising a storage tank of waste mother liquor in taurine industrial production, a parallel flow type drying tower 1, a cyclone separator 2, a liquid atomizing device, a heating air pipeline and a dust removal device (comprising a cloth bag dust removal device 3 and a water film dust removal device 4), wherein:
the storage tank of the waste mother liquor is communicated with the liquid atomization device through a pipeline, and the waste mother liquor can enter the drying tower after being atomized by the liquid atomization device and is contacted with heating air introduced by the heating air pipeline for atomization drying;
The inlet end of the cyclone separator 2 is communicated with the outlet of the drying tower, the exhaust end of the cyclone separator 2 is communicated with the dust removing device, the solid outlet c is connected with a storage tank of a mineral dressing regulator, the material inlet a of the parallel flow type drying tower and the hot air inlet b of the heating air pipeline are arranged at the top of the drying tower, and the bottom outlet of the drying tower is connected with the cyclone separator.
Example 5
This example provides a system for preparing a conditioning agent for beneficiation, as shown in FIG. 2, which system
The device comprises a storage tank for waste mother liquor in taurine industrial production, a convection type drying tower 1, a cyclone separator 2, a liquid atomization device, a heating air pipeline and a dust removal device (comprising a cloth bag dust removal device 3 and a water film dust removal device 4), wherein:
The storage tank of the waste mother liquor is communicated with the liquid atomization device through a pipeline, and the waste mother liquor can enter the drying tower 1 after being atomized by the liquid atomization device and is contacted with heating air introduced by the heating air pipeline for atomization drying;
The material inlet a of the convection type drying tower and the hot air inlet b of the heating air pipeline are respectively and oppositely arranged at the top and the bottom of the drying tower, and the top outlet of the drying tower is connected with the cyclone separator.
Test example 1:
The test example provides a mineral separation process, as shown in fig. 3. The raw ore is liquid taken from a copper ore discharge port, various medicaments are added into the raw ore, the raw ore is stirred and subjected to rough concentration, most of useful metals are settled to form rough concentrate, light solid and non-settled metals are separated to form suspension liquid, other medicaments are added into the suspension liquid for fine concentration, the useful metals in the liquid are settled to form a fine sweeping part, and the rest suspended matters and the liquid are discharged together, wherein the discharged matters are tailings.
Test example 2
Taking 525.8 g of liquid raw ore at a copper ore discharge port, adding 30 drops of kerosene, 30ml of water glass with the mass fraction of 10%, mechanically stirring for 5 minutes to roughen the obtained solid regulator (prepared in example 3) by spray drying at the air inlet temperature of 260 ℃, discharging suspended liquid, continuously concentrating, adding 3 drops of kerosene, 3 ml of water glass with the mass fraction of 10%, 2 g of water glass obtained by spray drying at the air inlet temperature of 260 ℃, mechanically stirring for 5 minutes to concentrate, settling useful metals in the liquid to form a clean part, discharging the rest suspended matters together with the liquid, and discharging the discharged matters as tailings. The metal content and recovery obtained from the experiment are shown in Table 4:
TABLE 4 Table 4
Test example 3
Taking 525.8 g of liquid crude ore at a copper ore discharge port, adding 30 drops of kerosene, 30ml of water glass with the mass fraction of 10%, 41.7 g of waste mother liquor, mechanically stirring for 5 minutes, carrying out rough concentration, continuously concentrating settled solids into coarse concentrate, adding 3 drops of kerosene, 3ml of water glass with the mass fraction of 10%, carrying out spray drying at the air inlet temperature of 260 ℃ for 2g of obtained solid regulator, mechanically stirring for 5 minutes, carrying out concentration, settling useful metals in the liquid to form a fine sweeping part, discharging the rest suspended matters and the liquid together, and discharging the discharged matters into tailings. The metal content and recovery obtained from the experiment are shown in Table 5:
TABLE 5
Test example 4
Taking 525.8 g of liquid raw ore at a copper ore discharge port, adding 30 drops of kerosene, 30 ml of water glass with the mass fraction of 10%, mechanically stirring for 5 minutes at an air inlet temperature of 150 ℃ to perform roughing, settling down the solid into rough concentrate, continuously concentrating suspended liquid, adding 3 drops of kerosene, 3 ml of water glass with the mass fraction of 10%, 2g of water glass with the mass fraction of 10%, spray-drying at the air inlet temperature of 150 ℃ to obtain solid, mechanically stirring for 5 minutes, concentrating, settling useful metals in the liquid to form a sweeping part, discharging the rest suspended matters together with the liquid, and discharging the suspended matters into tailings. The content and recovery rate of rare metal molybdenum obtained by the experiment are shown in Table 6:
TABLE 6
Test example 5
Taking 525.8 g of liquid crude ore at an ore discharge port, adding 30 drops of kerosene, 30 ml of water glass with the mass fraction of 10%, carrying out spray drying on 20 g of solid regulator (prepared in example 2) at the air inlet temperature of 200 ℃, mechanically stirring for 5 minutes, carrying out rough concentration, settling down the solid to be rough concentrate, continuously concentrating suspended liquid, adding 3 drops of kerosene, 3 ml of water glass with the mass fraction of 10%, carrying out spray drying on 2g of solid obtained at the air inlet temperature of 200 ℃, mechanically stirring for 5 minutes, carrying out concentration, settling useful metals in the liquid to form a sweeping part, discharging the rest suspended matters and the liquid together, and discharging the suspended matters to be tailings. The content and recovery rate of rare metal molybdenum obtained by the experiment are shown in Table 7:
TABLE 7
Test example 6
Taking 525.8 g of liquid raw ore at a copper ore discharge port, adding 30 drops of kerosene, 30 ml of water glass with the mass fraction of 10%, mechanically stirring 25 g of solid regulator (prepared in example 3) obtained by spray drying at the air inlet temperature of 260 ℃ for 5 minutes, carrying out roughing, settling down the solid to be rough concentrate, continuously concentrating suspended liquid, adding 3 drops of kerosene, 3 ml of water glass with the mass fraction of 10%, 2g of solid obtained by spray drying at the air inlet temperature of 260 ℃ for 5 minutes, mechanically stirring for concentrating, settling useful metals in the liquid to form a sweeping part, discharging the rest suspended matters together with the liquid, and discharging the suspended matters to be tailings. The content and recovery rate of rare metal molybdenum obtained by the experiment are shown in Table 8:
TABLE 8
From the above examples, it can be seen that the solids obtained by spray drying the spent mother liquor are suitable for flotation of rare metal molybdenum, and that the solids obtained by spray drying have a better selectivity for molybdenum than the spent mother liquor.
The above embodiments are merely preferred embodiments of the present application, and should not be construed as limiting the present application, and the embodiments and features of the embodiments of the present application may be arbitrarily combined with each other without collision. The protection scope of the present application is defined by the claims, and the protection scope includes equivalent alternatives to the technical features of the claims. I.e., equivalent replacement modifications within the scope of this application are also within the scope of the application.
Claims (11)
1. The preparation method of the conditioning agent for mineral separation is characterized by comprising the following steps of:
S1, atomizing waste mother liquor generated in industrial production of taurine into small liquid drops, wherein the waste mother liquor contains sodium isethionate, sodium taurate, glycol, ethanolamine and sodium sulfate, the content of the ethanolamine in the waste mother liquor is 0.1-10%, the content of the glycol is 0.1-10%, the content of the sodium taurate is 1-15%, the content of the sodium isethionate is 1-15%, and the content of the sodium sulfate is 5-55%;
S2, gasifying and removing the solvent and impurities with boiling points lower than the temperature of the hot air in the liquid drops by taking the hot air as a medium;
S3, collecting the solid formed after the obtained liquid drops are dried.
2. A beneficiation regulator in accordance with claim 1, wherein the droplets are contacted with the hot air in a parallel flow or a counter flow manner.
3. A beneficiation regulator in accordance with claim 1 or 2, wherein the atomization is performed in a centrifugal atomizer in a drying tower, the pressure in the spray drying tower is normal or negative pressure, and the spent mother liquor is pumped to the centrifugal atomizer at a feed rate of 1.0-100L/min.
4. A beneficiation process modifier according to claim 3, wherein the spent mother liquor is pumped to the centrifugal atomizer at a feed rate of 5-20L/min.
5. A mineral processing regulator according to claim 3, wherein the inlet volume flow rate of the hot air is 3000-20000m 3/h, the inlet volume flow rate is 3000-25000m 3/h, and the rotation speed of the centrifugal atomizer is 5000-20000rpm.
6. The mineral separation regulator according to claim 5, wherein the inlet volume flow rate of the hot air is 4500-20000m 3/h, the inlet volume flow rate is 6000-20000m 3/h, and the rotation speed of the centrifugal atomizer is 13000-16000rpm.
7. A beneficiation regulator in accordance with claim 1 or 2, wherein the hot air inlet temperature is 150-300 ℃ and/or the hot air outlet temperature is 50-150 ℃.
8. The beneficiation regulator in accordance with claim 7, wherein the inlet air temperature of the hot air is 250-270 ℃;
and/or the exhaust temperature of the hot air is 100-120 ℃.
9. The mineral separation regulator according to claim 1 or 2, wherein solid particles formed after drying the droplets are collected in step S3 by a cyclone, and cold air is introduced into the collection end of the cyclone.
10. A beneficiation regulator in accordance with claim 9, wherein the temperature of the cold air is in the range of-5 to 50 ℃.
11. The beneficiation regulator in accordance with claim 9, wherein the cold air is filtered through a filter.
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