A method and apparatus for preparing mineral processing modifiers

Abstract

This invention discloses a method and apparatus for preparing a mineral processing modifier. The method comprises the following steps: S1, atomizing waste mother liquor generated during taurine industrial production into small droplets; S2, vaporizing the solvent and low-boiling-point impurities in the small droplets using hot air as a medium; S3, collecting the solid formed after drying the droplets (which can be used directly or indirectly as a modifier in mineral processing reagents); the vapor from solvent vaporization is first collected by a bag filter to collect small particulate solids, and then purified by a water film filter. According to the treatment method provided by this invention, after spray drying, the content of impurities such as ethylene glycol and ethanolamine in the solid particles of the waste mother liquor is significantly reduced. The method of this invention treats waste mother liquor quickly, efficiently, and with a large processing capacity. The resulting solid particles can be used in mineral processing reagents. This green and environmentally friendly method for the rational utilization of waste mother liquor is suitable for industrial production.

Description

Technical Field

[0001] This invention relates to a method and apparatus for preparing mineral processing modifiers, belonging to the field of clean production of taurine. Background Technology

[0002] Taurine is a special amino acid found in living organisms. It has a wide range of physiological functions, such as promoting brain tissue and intellectual development in infants and young children, and enhancing cellular antioxidant capacity. Clinically, it has been widely used in the treatment of a range of diseases, including cardiovascular diseases, diabetes, digestive tract diseases, nervous system diseases, and eye diseases. Due to its widespread application, biological extraction methods can no longer meet human demand for taurine. Currently, over 90% of the taurine on the market comes from chemical synthesis methods, such as the ethanolamine method and the ethylene oxide method.

[0003] The ethanolamine method, due to its low yield, high synthesis cost, and long synthesis cycle, has been gradually replaced by the ethylene oxide method, which boasts higher yield, lower cost, and shorter cycle time. However, regardless of the chemical synthesis method used, corresponding byproducts will be generated. For example, in the industrial production of taurine using the ethylene oxide method, the waste mother liquor often contains incompletely extracted taurine, unreacted sodium hydroxyethyl sulfonate, byproducts such as sodium sulfate, ethylene glycol, ethanolamine, and its polymers.

[0004] The reaction formula for the preparation of taurine by the ethylene oxide method is as follows:

[0005]

[0006] The side reaction formula for the preparation of taurine by the ethylene oxide method is as follows:

[0007]

[0008] The reaction formula for the preparation of taurine by the ethanolamine method is as follows:

[0009] NH2CH2CH2OH+H2SO4→NH2CH2CH2OSO3H

[0010] NH2CH2CH2OSO3H+Na2SO3→NH2CH2CH2SO3H+Na2SO4

[0011] In the ethylene oxide process for preparing taurine, ethylene oxide reacts with water to produce ethylene glycol, which itself can polymerize to form polyethylene glycol (PEG). Ethylene glycol can further convert to ethanolamine during ammonolysis, and ethanolamine itself can also polymerize to form a polymer. In the ethanolamine process for taurine preparation, unreacted ethanolamine from the esterification reaction may polymerize to produce polyethanolamine. Additionally, 2-aminoethanol sulfate readily undergoes hydrolysis in the aqueous phase, producing ethanolamine.

[0012] In the preparation of taurine using the ethanolamine method, the sulfonation yield is low, so the unreacted ethanolamine undergoes polymerization to produce polyethanolamine. The taurine ester generated in the first step readily undergoes hydrolysis in the aqueous phase, producing ethanolamine and sulfuric acid.

[0013] Due to the large production capacity of taurine produced through chemical synthesis, the treatment of waste mother liquor from taurine industrial production is a crucial issue. Utilizing integrated wastewater treatment plants is a common wastewater treatment method in pharmaceutical companies, as illustrated by patent CN109761455A. This method offers advantages such as wide applicability and refined treatment steps, but it involves numerous steps, high costs, and the need for additional treatment agents. Recently, patent CN108128829A reported a device designed to achieve zero discharge of taurine industrial wastewater. This device first pre-treats the wastewater for desalination, then performs vaporization in a boiling vessel, adds liquid ammonia for conversion, and finally distills to achieve zero discharge. However, this device has a complex treatment route, requires the addition of low-boiling-point impurity scavengers, resulting in high costs and long treatment cycles, making it unsuitable for large-scale industrial production. Summary of the Invention

[0014] To address the above problems, this invention provides a method for rapidly and efficiently preparing mineral processing modifiers using waste mother liquor generated during taurine industrial production as raw material through spray drying.

[0015] Specifically, the method for preparing a mineral processing modifier provided by the present invention includes the following steps:

[0016] S1. Atomize the waste mother liquor generated in the industrial production of taurine into small droplets;

[0017] S2. Using heated air as a medium, vaporize to remove solvent and impurities with boiling points lower than the temperature of the heated air from the droplets;

[0018] S3. Collect the solid formed after the droplets are dried.

[0019] The solid (particles) obtained in step S3 above can be used as a modifier in the reagents for flotation beneficiation of copper ore. In order to improve its purity and quality, the method may further include purification operations for the modifier.

[0020] The waste mother liquor (also known as the material) originates from the process of producing taurine using ethylene oxide or ethanolamine as raw materials. Preferably, the waste mother liquor contains sodium hydroxyethyl sulfonate, sodium taurate, ethylene glycol, ethanolamine, and sodium sulfate. More preferably, the content of ethanolamine is 0.1%-10%, the content of ethylene glycol is 0.1-10%, the content of sodium taurate is 1%-15%, the content of sodium hydroxyethyl sulfonate is 1%-15%, and the content of sodium sulfate is 5%-55%.

[0021] The method described in this invention can transport the waste mother liquor to a centrifugal atomizer for the above-mentioned atomization using conventional techniques in the art. Preferably, the waste mother liquor is filtered before entering the drying tower, for example, by a filter.

[0022] In this process, air is heated by a heater to obtain hot air; preferably, the hot air is heated by a thermal oil heat exchanger, steam heating, an electric heater, or a combination of any two or three methods. Preferably, the air is filtered, for example, through a filter, before being heated and entering the drying tower.

[0023] Preferably, the contact mode between the small droplets of the waste mother liquor and the hot air is either parallel flow or convection flow.

[0024] In the parallel-flow contact method, the material enters the drying tower from the top of the tower. Hot air enters the tower tangentially from the upper side of the drying tower through the hot air distributor and flows in parallel with the material. When discharging, stronger air force is required to overcome the gravity of the material. Therefore, the equipment performance requirements are higher. Even if the material is highly viscous, it is not easy to clog the pipes, which is conducive to improving production efficiency.

[0025] In the convection contact method, the material enters the drying tower from the upper side of the drying tower. Hot air enters the drying tower from the bottom in a spiral shape through the hot air distributor and comes into convection contact with the material. At the same time, the material is sprayed out by the atomizer and falls under gravity, and then enters the hot air spiral upward again, which increases the heating time of the material, makes fuller use of heat energy, and makes the discharge more convenient.

[0026] Preferably, the droplet size obtained by atomization in step S1 is 1-1000 μm; more preferably 50-300 μm. This droplet size facilitates sufficient contact between the droplets and the hot air, thus improving drying efficiency.

[0027] Preferably, the feed rate of the waste mother liquor is 0.1-20 L / min; more preferably, it is 1-15 L / min. This feed rate can be matched with the capacity of the drying tower and the air inlet speed, which has the advantages of saving energy and improving production efficiency.

[0028] Preferably, the intake velocity of the hot air is:

[0029] The intake volume flow rate of the hot air is 3000-20000 m³ / h. 3 / h, preferably: 4500-20000m 3 / h; induced draft volumetric flow rate: 3000-25000 m³ / h 3 / h, preferably 6000-20000m 3 / h, the inlet air volume flow rate and the induced air volume flow rate are matched, which can create positive or negative pressure in the drying tower system, and has the advantages of quickly drying liquid and rapidly transferring the dried solid.

[0030] Preferably, the rotational speed of the centrifugal atomizer is 5000-20000 rpm; more preferably, it is 13000-16000 rpm. This rotational speed ensures the number of droplets formed and the required particle size, thus improving drying efficiency.

[0031] Preferably, the inlet temperature of the hot air is 150-300℃, more preferably 250-270℃. This inlet temperature ensures that both the solvent and low-boiling-point impurities are dried, offering advantages such as energy saving and high efficiency.

[0032] Preferably, the exhaust temperature of the hot air is 50-150℃, and more preferably 100-120℃.

[0033] Preferably, the waste mother liquor is atomized by centrifugal atomization or pressure atomization.

[0034] Preferably, the pressure inside the spray drying tower is atmospheric pressure or negative pressure. Hot air arrives at the drying tower via a blower, and the material exits the drying tower via an induced draft fan. When the blower speed and the induced draft fan speed are the same, the pressure inside the drying tower is atmospheric pressure; when the blower speed is lower than the induced draft fan speed, the pressure inside the drying tower is negative pressure.

[0035] Preferably, step S3 further includes introducing cold air into the collection end of the cyclone separator, preferably with a temperature of 0-40°C; preferably, the cold air is filtered through a filter. This cold air can come directly from room temperature air, which has the advantages of energy saving and efficiency improvement.

[0036] The purified air in step S4 of this invention can be directly discharged.

[0037] The present invention also provides a solid mixture (which can be used directly or indirectly as a modifier for mineral processing reagents) or a modifier for mineral processing reagents, which is prepared by the above method.

[0038] The solid obtained after spray drying of the waste mother liquor described in this invention (i.e., the modifier used in mineral processing reagents) contains specific amounts of sodium taurate, sodium hydroxyethyl sulfonate, sodium sulfate, and other substances. The amino groups in these substances can be used as cationic scavengers in mineral processing reagents, the sulfonic acid groups in organic compounds can be used as surfactants in mineral processing reagents, and the inorganic salts such as sodium sulfate can be used as modifiers in mineral processing reagents. The application effect is very outstanding.

[0039] This invention also provides a system for preparing a mineral processing modifier, comprising a storage tank for waste mother liquor from taurine industrial production, a drying tower, a cyclone separator, a liquid atomizing device, a heated air pipeline, and a dust removal device; wherein:

[0040] The waste mother liquor storage tank is connected to the liquid atomizing device through a pipeline. The waste mother liquor can be atomized by the liquid atomizing device and then enter the drying tower, where it comes into contact with the heated air introduced through the heated air pipeline for atomized drying.

[0041] The air inlet of the cyclone separator is connected to the outlet of the drying tower, the exhaust end is connected to the dust removal device, and the discharge port is connected to the storage tank of the mineral processing modifier.

[0042] In one embodiment of the present invention, the drying tower is a co-flow drying tower, particularly preferably a small LPG co-flow dryer, wherein the material inlet of the drying tower and the hot air inlet of the heating air duct are both located at the top of the drying tower, and the bottom outlet of the drying tower is connected to the cyclone separator.

[0043] 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 duct are respectively arranged opposite to each other at the top and bottom of the drying tower, and the top outlet of the drying tower is connected to the cyclone separator.

[0044] like Figure 1 As shown, in a co-flow drying tower, the material is pumped to a centrifugal atomizer inside the drying tower, atomized into small droplets, and then enters the drying tower from the top. The air is filtered by a filter and then heated by a heater. After entering the hot air distributor, the hot air enters the tower in a spiral shape from the upper part of the side of the drying tower in a tangential manner and comes into contact with the material.

[0045] The advantages of a co-flow drying tower are: the material and the heat source are in parallel flow contact, and a stronger air force is needed to overcome the gravity of the material when discharging. Therefore, the equipment performance requirements are higher. When the material is highly viscous, it is not easy to clog the pipes, thus improving production efficiency.

[0046] like Figure 2 As shown, in a convection drying tower, the material is pumped to a centrifugal atomizer inside the drying tower, atomized into small droplets, and then enters the drying tower from the upper part of the side. The air is filtered by a filter and then enters the heater for heating. After entering the hot air distributor, the hot air enters the drying tower in a spiral shape and enters evenly from the bottom of the drying tower. The material and the hot air come into contact in a convection manner.

[0047] The advantages of convection drying towers are: the material comes into contact with the heat source through convection, and the material is sprayed out by the atomizer and falls under gravity, and then enters the hot air spiral upward, which increases the heating time of the material, makes fuller use of heat energy, and makes the discharge more convenient.

[0048] This invention also provides a method for preparing mineral processing modifiers using the aforementioned apparatus. In use, air is filtered and then heated by a heater. The hot air enters a hot air distributor and then spirals uniformly into the drying tower. The liquid material, after being filtered, is pumped into a centrifugal atomizer inside the drying tower, where it is atomized into very small droplets. The material surface comes into contact with the hot air, causing rapid evaporation of moisture. Within a short time, the material is dried into solid particles. These particles are captured in a cyclone separator and a bag filter at the end of the tower. The particles captured at the end of the cyclone separator are cooled by cold air and then bagged. The wet exhaust gas is further purified by a water film dust collector before being discharged outdoors by a fan.

[0049] The mineral processing modifier preparation system of the present invention has the following characteristics:

[0050] 1. Fast drying speed: The liquid is centrifuged and sprayed, which greatly increases the surface area of ​​the droplets. In the high-temperature airflow, 95%-98% of the low-boiling-point solvents and impurities can be evaporated instantly, and the drying time can be completed in just a few seconds.

[0051] 2. Suitable for heat-sensitive materials. Because the droplets are in parallel or convective contact with the hot air, although the temperature of the hot air is high, the material will not overheat when the low-boiling-point solvent and impurities evaporate.

[0052] 3. It has a wide range of applications and can be used to produce a large number of materials with different physical properties, such as polymers and resins, pigments, glass, pesticides, dairy products, fertilizers, organic compounds, etc.

[0053] 4. This method is highly efficient and low-cost in treating large amounts of wastewater from industrial production, and effectively reduces the space required for waste disposal.

[0054] The mesh size of the solid particles processed by the method of the present invention is controlled by the feed rate and the rotation speed of the centrifugal atomizer, and the mesh size is 50-300 mesh, preferably 100-200 mesh.

[0055] The spray-dried solid was used as a reagent in flotation beneficiation. Experiments showed that the solid obtained by drying the mother liquor in the range of 250-280℃ had good selectivity for rare metal molybdenum ore. However, the effect of directly using the concentrated mother liquor as a reagent for beneficiating rare metal molybdenum was not as good as that of the solid.

[0056] The mineral processing principle of this invention may be as follows: the mother liquor treated by spray drying can partially remove the low-boiling-point solvent, leaving high-boiling-point sodium hydroxyethyl sulfonate with sulfonic acid groups and taurine. The sulfonic acid complexes with molybdenum to form a complex that floats on the surface of the liquid.

[0057] The beneficial effects of this invention are:

[0058] 1. Spray drying is a fast, efficient, and large-capacity method for treating waste mother liquor in taurine industrial production.

[0059] 2. As global mineral resources become increasingly scarce, lean and complex ores are being utilized more and more, resulting in a growing volume of ore requiring beneficiation. Mineral beneficiation can significantly improve the quality of mineral raw materials, reduce transportation costs, lower overall costs, and achieve comprehensive resource utilization.

[0060] 3. The mining and mineral processing industry requires large quantities of reagents and additives. The solid particles obtained after spray drying of waste mother liquor can be utilized in this industry, particularly for the selection of the rare metal molybdenum. This green and environmentally friendly method of rationally utilizing waste mother liquor is suitable for industrial production. Attached Figure Description

[0061] Figure 1 This is a schematic diagram of an apparatus for treating waste mother liquor in taurine industrial production, including a co-flow drying tower, according to the present invention.

[0062] Where a is the material inlet, b is the hot air inlet, and c is the solid outlet;

[0063] 1 is a co-flow drying tower; 2 is a cyclone separator; 3 is a bag filter; 4 is a water film filter.

[0064] Figure 2 This is a schematic diagram of an apparatus for treating waste mother liquor in taurine industrial production, including a convection drying tower, according to the present invention.

[0065] Where a is the material inlet, b is the hot air inlet, and c is the solid outlet;

[0066] 1 is a convection drying tower; 2 is a cyclone separator; 3 is a bag filter; 4 is a water film filter.

[0067] Figure 3 This invention provides a schematic diagram of the mineral processing flow for the solid obtained after treating waste mother liquor from taurine industrial production for use in mineral processing. Detailed Implementation

[0068] The present invention will be further illustrated below with reference to the embodiments. The following embodiments are used to illustrate the present invention, but are not intended to limit the scope of the present invention.

[0069] In the following examples, after the waste mother liquor was completely dried to obtain the mineral processing modifier, the solid content of the waste mother liquor was directly determined by the loss-in-weight method. Purified water was added to prepare a solution with the same concentration as the solid content of the waste mother liquor, and the residual ethylene glycol content was determined by chemical titration; the taurine content was determined by liquid chromatography; and the contents of ethanolamine and sodium hydroxyethyl sulfonate were determined by nuclear magnetic resonance internal standard method. The transmittance was detected by ultraviolet-visible spectrophotometry.

[0070] Example 1

[0071] This embodiment provides a method for treating waste mother liquor from taurine industrial production to obtain a mineral processing modifier, the method comprising the following steps:

[0072] S1. The waste mother liquor obtained from 1 ton of taurine industrial production is sent to the centrifugal atomizer in the XSG type convection drying tower and atomized into small droplets with a particle size of 0.3-100μm; wherein, the feed rate of the waste mother liquor is 50L / min;

[0073] S2. Hot air at a temperature of 150℃ is evenly introduced into the drying tower in a spiral pattern through a hot air distributor; wherein the inlet flow rate of the hot air is 4500 m³ / h. 3 / h; simultaneously, adjust the induced draft fan speed to 5000m 3 / h, creating negative pressure inside the drying chamber of the dryer;

[0074] S3. Collect the solid particles formed after the droplets are dried in the cyclone separator after the tower;

[0075] S4. The vapor from solvent vaporization is first collected by a bag filter to collect small particulate solids, and then purified by a water film filter.

[0076] The data measured in this embodiment are shown in Table 1:

[0077] Table 1

[0078]

[0079] Example 2

[0080] This embodiment provides a method for treating waste mother liquor from taurine industrial production, the method comprising the following steps:

[0081] S1. The waste mother liquor obtained from 1 ton of taurine industrial production is sent to the centrifugal atomizer in the XSG type convection drying tower and atomized into small droplets with a particle size of 0.3-100μm; wherein, the feed rate of the waste mother liquor is 50L / min;

[0082] S2. Hot air at a temperature of 200℃ is evenly introduced into the drying tower in a spiral pattern through a hot air distributor; wherein the inlet flow rate of the hot air is 5000 m³ / h. 3 / L; simultaneously, adjust the airflow of the induced draft fan to 6000m. 3 / L, creating negative pressure inside the dryer's drying chamber;

[0083] S3. Collect the solid particles formed after the droplets are dried in the cyclone separator after the tower;

[0084] S4. The vapor from solvent vaporization is first collected by a bag filter to collect small particulate solids, and then purified by a water film filter.

[0085] The data measured in this embodiment are shown in Table 2:

[0086] Table 2

[0087]

[0088] Example 3

[0089] This embodiment provides a method for treating waste mother liquor from taurine industrial production, the method comprising the following steps:

[0090] S1. The waste mother liquor obtained from 1 ton of taurine industrial production is sent to a centrifugal atomizer in an LPG-type co-flow drying tower and atomized into small droplets with a particle size of 0.3-100μm; wherein, the feed rate of the waste mother liquor is 100L / min;

[0091] S2. Hot air at a temperature of 260℃ is evenly introduced into the drying tower in a spiral pattern through a hot air distributor; wherein the inlet flow rate of the hot air is 5000 m³ / h. 3 / L; simultaneously, adjust the airflow of the induced draft fan to 6000m. 3 / L, creating negative pressure inside the dryer's drying chamber;

[0092] S3. Collect the solid particles formed after the droplets are dried in the cyclone separator after the tower;

[0093] S4. The vapor from solvent vaporization is first collected by a bag filter to collect small particulate solids, and then purified by a water film filter.

[0094] The data measured in this embodiment are shown in Table 3:

[0095] Table 3

[0096]

[0097] As can be seen from the above embodiments, the higher the inlet air temperature, the lower the content of ethylene glycol and ethanolamine in the dried solid, and the higher the light transmittance of the solution after dissolving in purified water. However, too high an inlet air temperature will have a negative impact on the equipment, such as high requirements for the equipment, which will lead to higher costs. Therefore, the preferred inlet air temperature is 260°C.

[0098] Example 4

[0099] This embodiment provides a system for preparing a mineral processing modifier, such as... Figure 1 As shown, the system includes a storage tank for waste mother liquor from taurine industrial production, a co-flow drying tower 1, a cyclone separator 2, a liquid atomizing device, heated air ducts, and dust removal devices (including a bag filter 3 and a water film filter 4); wherein:

[0100] The waste mother liquor storage tank is connected to the liquid atomizing device through a pipeline. The waste mother liquor can be atomized by the liquid atomizing device and then enter the drying tower, where it comes into contact with the heated air introduced through the heated air pipeline for atomized drying.

[0101] The air inlet of the cyclone separator 2 is connected to the outlet of the drying tower, the exhaust end is connected to the dust removal device, and the solid outlet c is connected to the storage tank of the mineral processing modifier; the material inlet a of the parallel flow drying tower and the hot air inlet b of the heating air pipeline are both located at the top of the drying tower, and the bottom outlet of the drying tower is connected to the cyclone separator.

[0102] Example 5

[0103] This embodiment provides a system for preparing a mineral processing modifier, such as... Figure 2 As shown, the system

[0104] This includes storage tanks for waste mother liquor from taurine industrial production, a convection drying tower 1, a cyclone separator 2, a liquid atomization device, heated air ducts, and dust collection devices (including a bag filter 3 and a water film filter 4); among which:

[0105] The waste mother liquor storage tank is connected to the liquid atomizing device through a pipeline. The waste mother liquor can be atomized by the liquid atomizing device and then enter the drying tower 1, where it comes into contact with the heated air introduced through the heated air pipeline for atomized drying.

[0106] The air inlet of the cyclone separator 2 is connected to the outlet of the drying tower, the exhaust end is connected to the dust removal device, and the solid outlet c is connected to the storage tank of the mineral processing modifier; the material inlet a of the convection drying tower and the hot air inlet b of the heating air pipeline are respectively arranged opposite to each other at the top and bottom of the drying tower, and the top outlet of the drying tower is connected to the cyclone separator.

[0107] Experimental Example 1:

[0108] This experimental example provides a mineral processing flow, such as... Figure 3As shown. The raw ore is a liquid taken from the copper mine outlet. After adding various reagents, it is stirred and roughed. Most of the useful metals settle to form a rough concentrate. The light solids and unsettled metals are separated to form a suspension. Other reagents are then added to the suspension for further cleaning, causing the useful metals in the liquid to settle to form a scavenging concentrate. The remaining suspended solids are discharged along with the liquid, and the discharge is called tailings.

[0109] Experimental Example 2

[0110] Take 525.8 grams of liquid raw ore from the copper ore outlet, add 30 drops of kerosene, 30 ml of 10% water glass, and 20 grams of a solid modifier obtained by spray drying at an inlet air temperature of 260°C (prepared in Example 3). Mechanically stir for 5 minutes for roughing. The settled solid is the rough concentrate. After the suspension is discharged, further refining is performed by adding 3 drops of kerosene, 3 ml of 10% water glass, and 2 grams of the solid obtained by spray drying at an inlet air temperature of 260°C. Mechanically stir for 5 minutes for refining. Useful metals in the liquid settle to form a clean fraction. The remaining suspended matter is discharged along with the liquid; the discharge is the tailings. The metal content and recovery rate obtained from the experiment are shown in Table 4.

[0111] Table 4

[0112]

[0113] Experimental Example 3

[0114] Take 525.8 grams of liquid raw ore from the copper ore outlet, add 30 drops of kerosene, 30 ml of 10% water glass, and 41.7 grams of waste mother liquor, and mechanically stir for 5 minutes for roughing. The settled solids are the rough concentrate. The suspension is further refined by adding 3 drops of kerosene, 3 ml of 10% water glass, and 2 grams of solid modifier obtained by spray drying at an inlet air temperature of 260℃. Mechanically stir for 5 minutes for further refining. The useful metals in the liquid settle to form the scavenged concentrate. The remaining suspended solids are discharged together with the liquid, and the discharge is the tailings. The metal content and recovery rate obtained from the experiment are shown in Table 5.

[0115] Table 5

[0116]

[0117]

[0118] Test Example 4

[0119] Take 525.8 grams of liquid raw ore from the copper ore outlet, add 30 drops of kerosene, 30 ml of 10% water glass, and 20 grams of a solid modifier (prepared in Example 1) obtained by spray drying at an inlet air temperature of 150°C. Mechanically stir for 5 minutes for roughing. The settled solid is the rough concentrate. Continue cleaning the suspension by adding 3 drops of kerosene, 3 ml of 10% water glass, and 2 grams of the solid obtained by spray drying at an inlet air temperature of 150°C. Mechanically stir for 5 minutes for cleaning. Useful metals in the liquid settle to form a clean fraction. The remaining suspended matter is discharged along with the liquid; the discharge is the tailings. The content and recovery rate of the rare metal molybdenum obtained in the experiment are shown in Table 6.

[0120] Table 6

[0121]

[0122] Experimental Example 5

[0123] Take 525.8 grams of liquid ore from the ore outlet, add 30 drops of kerosene, 30 ml of 10% water glass, and 20 grams of a solid modifier (prepared in Example 2) obtained by spray drying at an inlet air temperature of 200°C. Stir mechanically for 5 minutes for roughing. The settled solid is the rough concentrate. Continue fine cleaning of the suspension by adding 3 drops of kerosene, 3 ml of 10% water glass, and 2 grams of the solid obtained by spray drying at an inlet air temperature of 200°C. Stir mechanically for 5 minutes for fine cleaning. Useful metals in the liquid settle to form a clean fraction. The remaining suspended matter is discharged along with the liquid; the discharge is the tailings. The content and recovery rate of the rare metal molybdenum obtained in the experiment are shown in Table 7.

[0124] Table 7

[0125]

[0126] Experimental Example 6

[0127] Take 525.8 grams of liquid raw ore from the copper ore outlet, add 30 drops of kerosene, 30 ml of 10% water glass, and 25 grams of a solid modifier obtained by spray drying at an inlet air temperature of 260°C (prepared in Example 3). Mechanically stir for 5 minutes for roughing. The settled solid is the rough concentrate. Continue cleaning the suspension by adding 3 drops of kerosene, 3 ml of 10% water glass, and 2 grams of the solid obtained by spray drying at an inlet air temperature of 260°C. Mechanically stir for 5 minutes for cleaning. Useful metals in the liquid settle to form a clean fraction. The remaining suspended matter is discharged along with the liquid; the discharge is the tailings. The content and recovery rate of the rare metal molybdenum obtained in the experiment are shown in Table 8.

[0128] Table 8

[0129]

[0130] As can be seen from the above examples, the solid obtained by spray drying of waste mother liquor is suitable for flotation of rare metal molybdenum, and the solid after spray drying has better selectivity for molybdenum than that of waste mother liquor.

[0131] The above embodiments are merely preferred technical solutions of the present invention and should not be considered as limitations on the present invention. The embodiments and features described in these embodiments can be arbitrarily combined without conflict. The scope of protection of the present invention should be limited to the technical solutions described in the claims, including equivalent substitutions of the technical features described in the claims. That is, equivalent substitutions and improvements within this scope are also within the scope of protection of the present invention.

Claims

1. A mineral processing modifier, characterized in that, The preparation method of the mineral processing modifier includes the following steps: S1. Atomize the waste mother liquor generated in the industrial production of taurine into small droplets; the waste mother liquor contains sodium hydroxyethyl sulfonate, sodium taurate, ethylene glycol, ethanolamine, and sodium sulfate; the content of ethanolamine in the waste mother liquor is 0.1%-10%, the content of ethylene glycol is 0.1-10%, the content of sodium taurate is 1%-15%, the content of sodium hydroxyethyl sulfonate is 1%-15%, and the content of sodium sulfate is 5%-55%; S2. Using hot air as a medium, vaporize to remove the solvent and impurities with boiling points lower than the temperature of the hot air from the droplets; S3. Collect the solid formed after the droplets are dried.

2. The mineral processing modifier according to claim 1, characterized in that, The contact between the small droplets and the hot air is either parallel flow or convection.

3. The mineral processing modifier according to claim 1 or 2, characterized in that, The atomization is carried out in a centrifugal atomizer inside the drying tower. The pressure inside the spray drying tower is atmospheric pressure or negative pressure. The waste mother liquor is pumped to the centrifugal atomizer at a feed rate of 1.0-100L / min.

4. The mineral processing modifier according to claim 3, characterized in that, Waste mother liquor is pumped to a centrifugal atomizer at a feed rate of 5-20 L / min.

5. The mineral processing modifier according to claim 3, characterized in that, The intake volume flow rate of the hot air is 3000-20000 m³ / h. 3 / h; induced draft volumetric flow rate is 3000-25000 m³ / h. 3 / h; the rotational speed of the centrifugal atomizer is 5000-20000 rpm.

6. The mineral processing modifier according to claim 5, characterized in that, The intake volume flow rate of the hot air is 4500-20000 m³ / h. 3 / h; induced draft volumetric flow rate is 6000-20000 m³ / h. 3 / h; the rotational speed of the centrifugal atomizer is 13000-16000 rpm.

7. The mineral processing modifier according to claim 1 or 2, characterized in that, The inlet temperature of the hot air is 150-300℃; and / or, the outlet temperature of the hot air is 50-150℃.

8. The mineral processing modifier according to claim 7, characterized in that, The inlet temperature of the hot air is 250-270℃; And / or, the exhaust temperature of the hot air is 100-120°C.

9. The mineral processing modifier according to claim 1 or 2, characterized in that, In step S3, a cyclone separator is used to collect the solid particles formed after the droplets are dried, and cold air is introduced into the collection end of the cyclone separator.

10. The mineral processing modifier according to claim 9, characterized in that, The temperature of the cold air is -5 to 50°C.

11. The mineral processing modifier according to claim 9, characterized in that, The cold air is filtered by a filter.

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