CN119464771A - A system and method for improving the leaching rate of low-grade scheelite - Google Patents
A system and method for improving the leaching rate of low-grade scheelite Download PDFInfo
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- CN119464771A CN119464771A CN202510052364.2A CN202510052364A CN119464771A CN 119464771 A CN119464771 A CN 119464771A CN 202510052364 A CN202510052364 A CN 202510052364A CN 119464771 A CN119464771 A CN 119464771A
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- 238000002386 leaching Methods 0.000 title claims abstract description 54
- 238000000034 method Methods 0.000 title claims abstract description 26
- 229910052500 inorganic mineral Inorganic materials 0.000 claims abstract description 40
- 239000011707 mineral Substances 0.000 claims abstract description 40
- 238000004537 pulping Methods 0.000 claims abstract description 33
- 239000000843 powder Substances 0.000 claims abstract description 29
- 238000000926 separation method Methods 0.000 claims abstract description 28
- 239000007788 liquid Substances 0.000 claims abstract description 26
- 238000000227 grinding Methods 0.000 claims abstract description 10
- 230000008569 process Effects 0.000 claims abstract description 10
- 238000009835 boiling Methods 0.000 claims abstract description 9
- 230000003213 activating effect Effects 0.000 claims abstract description 7
- 239000000725 suspension Substances 0.000 claims description 23
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 18
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 15
- 239000012141 concentrate Substances 0.000 claims description 13
- WFKWXMTUELFFGS-UHFFFAOYSA-N tungsten Chemical compound [W] WFKWXMTUELFFGS-UHFFFAOYSA-N 0.000 claims description 13
- 229910052721 tungsten Inorganic materials 0.000 claims description 13
- 239000010937 tungsten Substances 0.000 claims description 13
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 9
- 239000002518 antifoaming agent Substances 0.000 claims description 8
- 239000000395 magnesium oxide Substances 0.000 claims description 8
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 claims description 8
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 claims description 8
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 claims description 6
- 239000003795 chemical substances by application Substances 0.000 claims description 6
- 239000000203 mixture Substances 0.000 claims description 6
- 229910052710 silicon Inorganic materials 0.000 claims description 6
- 239000010703 silicon Substances 0.000 claims description 6
- 239000007787 solid Substances 0.000 claims description 6
- 239000002002 slurry Substances 0.000 claims description 5
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 claims description 4
- 239000000292 calcium oxide Substances 0.000 claims description 4
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 claims description 4
- 239000008394 flocculating agent Substances 0.000 claims description 4
- DIZPMCHEQGEION-UHFFFAOYSA-H aluminium sulfate (anhydrous) Chemical compound [Al+3].[Al+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O DIZPMCHEQGEION-UHFFFAOYSA-H 0.000 claims description 3
- 238000003801 milling Methods 0.000 claims description 3
- WNROFYMDJYEPJX-UHFFFAOYSA-K aluminium hydroxide Chemical compound [OH-].[OH-].[OH-].[Al+3] WNROFYMDJYEPJX-UHFFFAOYSA-K 0.000 claims description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 2
- 229910052760 oxygen Inorganic materials 0.000 claims description 2
- 239000001301 oxygen Substances 0.000 claims description 2
- 238000004321 preservation Methods 0.000 claims description 2
- 239000000126 substance Substances 0.000 claims description 2
- 238000011084 recovery Methods 0.000 abstract description 11
- 229910052751 metal Inorganic materials 0.000 abstract description 8
- 239000002184 metal Substances 0.000 abstract description 8
- 239000000463 material Substances 0.000 abstract description 3
- 230000004913 activation Effects 0.000 abstract description 2
- 238000004134 energy conservation Methods 0.000 abstract description 2
- 230000009467 reduction Effects 0.000 abstract description 2
- 239000002893 slag Substances 0.000 description 18
- 230000000052 comparative effect Effects 0.000 description 10
- 238000010411 cooking Methods 0.000 description 4
- 229920002401 polyacrylamide Polymers 0.000 description 3
- 238000005352 clarification Methods 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005259 measurement Methods 0.000 description 2
- 238000005070 sampling Methods 0.000 description 2
- 238000011144 upstream manufacturing Methods 0.000 description 2
- 238000005303 weighing Methods 0.000 description 2
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 238000009854 hydrometallurgy Methods 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000007873 sieving Methods 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B34/00—Obtaining refractory metals
- C22B34/30—Obtaining chromium, molybdenum or tungsten
- C22B34/36—Obtaining tungsten
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B1/00—Preliminary treatment of ores or scrap
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B1/00—Preliminary treatment of ores or scrap
- C22B1/02—Roasting processes
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
- C22B3/02—Apparatus therefor
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
- C22B3/04—Extraction of metal compounds from ores or concentrates by wet processes by leaching
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
- C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
- C22B3/22—Treatment or purification of solutions, e.g. obtained by leaching by physical processes, e.g. by filtration, by magnetic means, or by thermal decomposition
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Mechanical Engineering (AREA)
- Manufacturing & Machinery (AREA)
- Materials Engineering (AREA)
- Metallurgy (AREA)
- Organic Chemistry (AREA)
- Geochemistry & Mineralogy (AREA)
- Geology (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Life Sciences & Earth Sciences (AREA)
- Manufacture And Refinement Of Metals (AREA)
Abstract
The application discloses a system and a method for improving the leaching rate of low-grade scheelite, which relate to the technical field of mineral recovery and specifically comprise the following steps of S1, roasting and deslagging; S2, pulping, S2, crushing and activating by a vertical mill, S5, pressure boiling and leaching, S6, primary solid-liquid separation, S7, enrichment, and S8, secondary solid-liquid separation. According to the technical scheme of the cyclone and vertical mill cooperation in the system, the heavy and light phases are separated, the efficiency of the vertical mill is improved, the activation energy is increased for ore pulp after ore grinding, the leaching reaction is facilitated, the yield of the whole process is improved, valuable metal enrichment of low-grade raw ore can be realized, the consumption of raw and auxiliary materials is low, the solid-liquid separation and enrichment are carried out for many times, the enriched mineral powder and backwater are returned to the front section for reuse, and the energy conservation and the emission reduction are realized.
Description
Technical Field
The invention relates to the technical field of mineral recovery, in particular to a system and a method for improving the leaching rate of low-grade scheelite.
Background
Tungsten is used as refractory rare heavy metal, the current common hydrometallurgy method is sodium carbonate leaching, but because more complex beneficiation reagent is added in the beneficiation process, the influence on subsequent leaching is larger due to incomplete deslagging and the nature of ore in the roasting deslagging process, the current mature process can only ensure that leaching residues are about 0.5 percent, still partial leaching residues exceed 1 percent and even higher, the currently used mineral powder is partially agglomerated in the roasting process, the passing through a 60-mesh sieve can reach 99 percent, the passing through a 200-mesh sieve can reach more than 8 percent, the leaching effect is also directly influenced, the incomplete mineral powder is treated with the leaching residues according to dangerous waste, valuable metal loss is caused, and the leaching rate is greatly influenced.
Disclosure of Invention
The invention aims to overcome the defects of the prior art and provide a system and a method for improving the leaching rate of low-grade scheelite and improving the leaching rate of mineral powder.
The technical scheme adopted by the invention is as follows:
A system for improving leaching rate of low-grade scheelite comprises a roasting furnace, a pulping tank, a cyclone, a vertical mill, an autoclave, a storage tank, a filter press I, a blanket machine, a suspension machine enrichment and a filter press II;
The roasting furnace outlet is connected with a feeding port of a pulping tank through a conveyor, the pulping tank outlet is connected with a cyclone inlet through a pump, a light phase outlet of the cyclone is connected with an inlet of an autoclave, a heavy phase outlet of the cyclone is connected with a connecting port of a vertical mill, the outlet of the vertical mill is connected with the inlet of the autoclave through a pump, the outlet of the autoclave is connected with an inlet of a storage tank, the outlet of the storage tank is connected with an inlet of a filter press I through a pump, a leaching residue outlet of the filter press I is connected with a slurry mixing tank inlet, a slurry mixing tank outlet is connected with a mineral inlet of a blanket machine, a coarse concentrate outlet of the blanket machine is connected with a mineral inlet of a suspension machine, a concentrate outlet of the suspension machine is connected with an inlet of the filter press II, a mineral powder outlet of the filter press II is connected with the pulping tank, and a water outlet is connected into the leaching residue tank of the filter press I through a pipeline.
A method for improving the leaching rate of low-grade scheelite comprises the following specific steps:
the method comprises the steps of S1, roasting and deslagging, wherein the raw ore grade is 22-30% of WO 3 in terms of weight percent, the moisture content is 10-15% of WO 3, the raw ore grade enters a roasting furnace for roasting and deslagging, the roasting temperature is 500-750 ℃, the roasting time is 0.5-2 hours, the COD (chemical oxygen demand) after roasting is less than or equal to 500mg/L, and the moisture is not more than 0.1%;
S2, pulping, namely adding water into the roasted mineral powder to carry out pulping, wherein the liquid-solid ratio of the water to the mineral powder is 3-5:1, adding sodium carbonate solid with the content of more than or equal to 98% and a silicon removing agent in the pulping process, and the concentration of sodium carbonate after pulping is 130-220g/L;
s3, splitting by a cyclone, conveying the ore pulp prepared by the step S2 to the cyclone through a pump, enabling the light phase split by the cyclone to enter an autoclave, and enabling the heavy phase to enter a vertical mill;
S4, crushing and activating a vertical mill, wherein heavy phase is crushed and activated in the vertical mill, the ore grinding time is not less than 30min, the passing rate of mineral granularity-60 meshes is more than 95%, and the ore pulp after vertical milling is conveyed to an autoclave through a pump;
S5, pressure boiling and leaching, wherein the light phase split by the cyclone in S3 and the ore pulp after the S4 vertical mill are subjected to pressure boiling and leaching in a pressure boiling kettle, the pressure boiling temperature is controlled to be 185-220 ℃, and the mixture is discharged to a storage tank after heat preservation is carried out for 0.5-2 hours;
s6, carrying out primary solid-liquid separation, wherein ore pulp in the storage tank is conveyed to a filter press I through a pump for solid-liquid separation, and the separated valuable tungsten-containing solution enters a subsequent workshop for treatment;
S7, enriching, namely adding an antifoaming agent into leached residues in the S6, pulping, wherein the pulp concentration is less than or equal to 20% by weight, and the pulp enters a blanket machine for primary enrichment after pulp mixing, and coarse concentrate of the blanket machine enters a suspension machine for secondary enrichment;
And S8, carrying out secondary solid-liquid separation, wherein the concentrate of the suspension machine enters a filter press II for solid-liquid separation, the mineral powder of the filter press II returns to the S2, and the return water is added with a flocculating agent to enter the S7 for leaching residues for size mixing.
Specifically, the silicon removing agent in S2 is one or more of magnesium oxide with the content of more than or equal to 85 percent, industrial aluminum sulfate and industrial aluminum hydroxide with the content of more than or equal to 64.5 percent in percentage by weight, and the adding amount of the silicon removing agent is 3-5 percent of the weight of mineral powder respectively.
More specifically, the content of calcium oxide in the magnesium oxide is lower than 5%.
Specifically, in the step S7, the adding amount of the antifoaming agent is 3 ‱ of the total solution volume.
Specifically, the flocculant adding amount in the step S8 is used for supplementing polyacrylamide according to the turbidity of water, and the turbidity requirement is less than or equal to 70mg/L.
By adopting the technical scheme, the invention has the following advantages:
According to the technical scheme of the cyclone and vertical mill cooperation in the system, the heavy and light phases are separated, the efficiency of the vertical mill is improved, the activation energy is increased for ore pulp after ore grinding, the leaching reaction is facilitated, the yield of the whole process is improved, valuable metal enrichment of low-grade raw ore can be realized, the consumption of raw and auxiliary materials is low, the solid-liquid separation and enrichment are carried out for many times, the enriched mineral powder and backwater are returned to the front section for reuse, and the energy conservation and the emission reduction are realized.
Drawings
Fig. 1 is a schematic flow chart of the present invention.
Detailed Description
The present invention is further explained below with reference to the drawings and examples, which are not to be construed as limiting the scope of the invention, and the purpose of the present invention is to protect all technical improvements within the scope of the invention.
The system for improving the leaching rate of the low-grade scheelite shown in the attached figure 1 comprises a roasting furnace, a pulping tank, a cyclone, a vertical mill, an autoclave, a storage tank, a filter press I, a blanket machine, a suspension machine enrichment and a filter press II;
The roasting furnace outlet is connected with a feeding port of a pulping tank through a conveyor, the pulping tank outlet is connected with a cyclone inlet through a pump, a light phase outlet of the cyclone is connected with an inlet of an autoclave, a heavy phase outlet of the cyclone is connected with a connecting port of a vertical mill, the outlet of the vertical mill is connected with the inlet of the autoclave through a pump, the outlet of the autoclave is connected with an inlet of a storage tank, the outlet of the storage tank is connected with an inlet of a filter press I through a pump, an outlet of a slag leaching tank of the filter press I is connected with an inlet of a pulp mixing tank, an outlet of the pulp mixing tank is connected with an ore inlet of a blanket machine, a coarse concentrate outlet of the blanket machine is connected with an ore inlet of a suspension machine, a concentrate outlet of the suspension machine is connected with an inlet of a filter press II, and an ore powder outlet of the filter press II is connected with the pulping tank through a pipeline.
Example 1
A method for improving the leaching rate of low-grade scheelite comprises the following specific steps:
S1, roasting and deslagging, wherein the grade of discharged raw ore of an upstream mineral separation unit filter press is 22% in terms of weight fraction, the moisture is 10%, the raw ore enters a roasting furnace at a rate of 3t/h for roasting and deslagging, the roasting temperature is 500 ℃ for 2 hours, the grade of roasted mineral powder is 22.05% in terms of WO 3, the moisture is 0.02%, and the COD is 500mg/L.
S2, pulping, namely adding 3 tons of baked mineral powder into a 20-cube pulping tank, mixing with 15 cubes of water, adding 1970 kg of sodium carbonate solid with the content of more than or equal to 98% in the pulping process to ensure that the concentration of sodium carbonate is 130 g/L, adding 105.88 kg of magnesium oxide with the content of more than or equal to 85% according to the weight of 3% of the mineral powder, wherein the content of calcium oxide in the magnesium oxide is lower than 5%, and sampling ore pulp after pulping and sieving with a 60-mesh sieve to obtain the pulp with the passing rate of 72.50%.
S3, splitting by a cyclone, conveying the ore pulp prepared by the step S2 to the cyclone through a pump, enabling the light phase split by the cyclone to enter an autoclave, and enabling the heavy phase to enter a vertical mill.
S4, crushing and activating the heavy phase in a vertical mill, crushing and activating the heavy phase in the vertical mill for 30min, enabling the passing rate of the ore granularity of-60 meshes to be 95.24%, meeting the technological requirements after grinding, prolonging the grinding time if detecting that the passing rate of the ore passing rate of 60 meshes is less than or equal to 95%, and conveying qualified ore pulp after vertical milling to an autoclave through a pump.
And S5, carrying out pressure cooking leaching on the light phase split by the cyclone in S3 and the ore pulp subjected to the S4 vertical mill in an autoclave, controlling the pressure cooking temperature at 185 ℃, preserving the heat for 2 hours, and discharging the mixture to a storage tank.
S6, carrying out solid-liquid separation once, conveying ore pulp in a storage tank to a filter press I through a pump for solid-liquid separation, calculating the dry weight of leaching residues to be 2.4 tons through on-site measurement and weighing, measuring the content of WO 3 in the leaching residues to be 0.53 percent, and obtaining the recovery rate of 98.077 percent by a residue meter, wherein the separated valuable tungsten-containing solution enters a subsequent workshop for treatment.
S7, enriching, namely adding a defoaming agent into the leached residues in S6 after entering a pulp mixing barrel, adding the defoaming agent into the leached residues according to the total solution volume of 3 ‱, wherein the concentration of the mixed pulp is 20% by weight, entering a blanket machine for primary enrichment after pulp mixing, wherein the blanket machine is 100 paths of blanket with the width of 1.0 meter and the length of 9.5 meters, and entering two XFJ-30 suspension machines connected in parallel for secondary enrichment;
The leaching slag with the content of 0.53% of 200 tons of WO 3 is enriched by a blanket machine and a suspension machine to obtain 2.1 tons of enriched mineral powder with the content of 18.20%, the moisture is 19.85%, the direct yield of metal tungsten passing through the blanket machine and the suspension machine is proved to be 28.90%, the grade of tungsten in tailings is 0.37%, the influence on the total-stage yield is that the direct yield (slag meter) is increased by 0.581%, and the total-stage yield reaches 98.658%.
And S8, carrying out secondary solid-liquid separation, wherein the concentrate secondarily enriched by the suspension machine enters a filter press II for solid-liquid separation, the mineral powder prepared by the filter press II returns to S2, the returned water is added with a flocculating agent polyacrylamide for clarification, and the mixture enters S7 for leaching residues for size mixing after the turbidity requirement is less than or equal to 70 mg/L.
Comparative example 1
The pulp after pulping in the step S2 of the example 1 directly enters an autoclave and reacts for 2.0 hours at 185 ℃ and is discharged and enters a filter press for solid-liquid separation to obtain leaching residue WO 3 with the content of 0.80 percent, the recovery rate of the direct autoclave slag meter is 97.098 percent, compared with the recovery rate of the slag meter of the S6 in the example 1, the scheme of the example 1 recovers more tungsten by 6.48 kilograms, and the yield of the example 1 is improved by 0.979 percent compared with the yield of the comparative example 1.
200 Tons of 0.80% leaching slag of comparative example 1 is taken, and in the same way, in the step S7 of example 1, 4.2 tons of 15.63% enriched mineral powder is obtained after enrichment by a suspension machine and a blanket machine, the moisture is 20.25%, the direct yield of metal tungsten through the blanket machine and the suspension machine is checked to be 32.72%, the grade of tungsten in the tailings is 0.42%, the effect on the total yield is that the direct yield (slag meter) is increased by 1.378%, and the total yield is 98.476%. Table 1 shows the summary of the yield data of example 1 and comparative example 1.
TABLE 1
| Category(s) | Content of leached slag by primary solid-liquid separation | Direct recovery rate of primary solid-liquid separation slag | Enrichment increases the direct yield of the whole section | Total direct yield |
| Comparative example 1 | 0.80% | 97.098% | 1.378% | 98.476% |
| Example 1 | 0.53% | 98.077% | 0.581% | 98.658% |
Example 2
A method for improving the leaching rate of low-grade scheelite comprises the following specific steps:
S1, roasting and deslagging, wherein the grade of discharged raw ore of an upstream mineral separation unit filter press is 30% in terms of weight fraction, the moisture is 15%, the raw ore enters a roasting furnace at a rate of 3t/h for roasting and deslagging, the roasting temperature is 750 ℃ for 0.5 hour, the grade of the roasted mineral powder is 30.09%, the moisture is 0.02%, and the COD is 500mg/L.
S2, pulping, namely adding 3 tons of baked mineral powder into a 20-cube pulping tank, mixing the slurry with 9 cubes of water, adding 2020.41 kg of sodium carbonate solid with the content of more than or equal to 98% in the pulp mixing process to ensure that the concentration of sodium carbonate is 220 g/L, adding 105.88 kg of magnesium oxide with the content of more than or equal to 85% according to the weight of the mineral powder, wherein the content of calcium oxide in the magnesium oxide is lower than 5%, adding aluminum sulfate with the content of more than or equal to 64.5% according to the weight of the mineral powder by 3%, and 139.53 kg of water, and sampling the pulp after pulping, and passing through a 60-mesh sieve with the passing rate of 77.86%.
S3, splitting by a cyclone, conveying the ore pulp prepared by the step S2 to the cyclone through a pump, enabling the light phase split by the cyclone to enter an autoclave, and enabling the heavy phase to enter a vertical mill.
S4, crushing and activating a vertical mill, crushing and activating heavy phase in the vertical mill, grinding for 30min, enabling the passing rate of the mineral granularity to be-60 meshes to be 96.20%, meeting the technological requirements after grinding, if the passing rate of the mineral granularity to be-60 meshes is detected to be less than or equal to 95%, prolonging the grinding time, and conveying the ore pulp after vertical grinding to an autoclave through a pump.
And S5, carrying out pressure cooking leaching on the light phase split by the cyclone in S3 and the ore pulp subjected to the S4 vertical mill in an autoclave, controlling the pressure cooking temperature to be 220 ℃, preserving the heat for 0.5 hour, and discharging the mixture to a storage tank.
S6, carrying out solid-liquid separation once, conveying ore pulp in a storage tank to a filter press I through a pump for solid-liquid separation, carrying out on-site measurement weighing, calculating the dry weight of leaching residues to be 2.4 tons, measuring the content of WO 3 in the leaching residues to be 0.36 percent, and carrying out slag recovery rate to be 99.04 percent, wherein the separated valuable tungsten-containing solution enters a subsequent workshop for treatment.
S7, enriching, namely adding the leached residues into a pulp mixing barrel, adding an antifoaming agent for pulp mixing, adding the antifoaming agent into the pulp mixing barrel according to the total solution volume of 3 ‱, adding the pulp mixing concentration of 20% by weight, adding the pulp into a blanket machine for primary enrichment after pulp mixing, adding the blanket machine into a blanket 100-channel with the width of 1.0 m and the length of 9.5 m, adding coarse concentrate of the blanket machine into two parallel XFJ-30 suspension machines for secondary enrichment, and adding tailings obtained by the secondary enrichment into a tailing pond.
The leaching slag with the content of 0.36 percent of 200 tons of WO 3 is enriched by a blanket machine and a suspension machine to obtain 1.25 tons of enriched mineral powder with the content of 22.08 percent, the moisture is 17.95 percent, the direct yield of the metal tungsten is checked to be 31.45 percent, the tailings grade is 0.23 percent, the influence on the total section yield is that the direct yield (slag gauge) is increased by 0.35 percent, and the total section yield reaches 99.39 percent.
And S8, carrying out secondary solid-liquid separation, wherein the concentrate of the suspension machine enters a filter press II for solid-liquid separation, the mineral powder of the filter press II returns to the S2, the returned water is added with a flocculating agent polyacrylamide for clarification, and the mixture enters the S7 for leaching residues for size mixing after the turbidity requirement is less than or equal to 70 mg/L.
Comparative example 2
The pulp after pulping in the step S2 of the example 2 directly enters an autoclave and reacts for 0.5 hour at 220 ℃, the discharged material is directly subjected to solid-liquid separation by a filter press to obtain leaching residue WO 3 with the content of 0.63%, the recovery rate of a direct autoclave slag meter is 98.32%, compared with the recovery rate of the slag meter of the S6 in the example 2, the scheme of the example 2 is used for recovering 6.48 kg of tungsten, and the yield of the example 2 is improved by 0.72% compared with that of the comparative example 2.
Based on 200 tons of leaching slag with the WO 3 content of 0.63% in comparative example 2, and also based on step S7 of example 2, enriched mineral powder with the WO 3 content of 18.20% is obtained after enrichment by a suspension machine and a blanket machine, wherein the moisture content is 18.88%, the direct yield of the proved metal tungsten is 31.64%, the tailings grade is 0.42%, the influence on the total-stage yield is that the direct yield (slag gauge) is increased by 0.56%, and the total-stage yield reaches 98.88%. Table 2 is a summary of the yield data for example 2 and comparative example 2.
TABLE 2
| Category(s) | Content of leached slag by primary solid-liquid separation | Direct recovery rate of primary solid-liquid separation slag | Enrichment increases the direct yield of the whole section | Total direct yield |
| Comparative example 2 | 0.63% | 98.32% | 0.56% | 98.88% |
| Example 2 | 0.36% | 99.04% | 0.35% | 99.39% |
The technical scheme of the invention is that compared with the technical scheme of directly feeding the leaching residue into the autoclave for leaching after pulping, the technical scheme of the invention is used for recycling valuable metals from low-grade raw ores, and the direct recovery rate is improved to a greater extent.
The invention is not described in detail in the prior art.
The embodiments selected herein for the purposes of disclosing the invention are presently considered to be suitable, but it is to be understood that the invention is intended to include all such variations and modifications as fall within the spirit and scope of the invention.
Claims (6)
1. A system for improving the leaching rate of low-grade scheelite is characterized by comprising a roasting furnace, a pulping tank, a cyclone, a vertical mill, an autoclave, a storage tank, a filter press I, a blanket machine, a suspension machine enrichment and a filter press II;
The roasting furnace outlet is connected with a feeding port of a pulping tank through a conveyor, the pulping tank outlet is connected with a cyclone inlet through a pump, a light phase outlet of the cyclone is connected with an inlet of an autoclave, a heavy phase outlet of the cyclone is connected with a connecting port of a vertical mill, the outlet of the vertical mill is connected with the inlet of the autoclave through a pump, the outlet of the autoclave is connected with an inlet of a storage tank, the outlet of the storage tank is connected with an inlet of a filter press I through a pump, a leaching residue outlet of the filter press I is connected with a slurry mixing tank inlet, a slurry mixing tank outlet is connected with a mineral inlet of a blanket machine, a coarse concentrate outlet of the blanket machine is connected with a mineral inlet of a suspension machine, a concentrate outlet of the suspension machine is connected with an inlet of the filter press II, a mineral powder outlet of the filter press II is connected with the pulping tank, and a water outlet is connected into the leaching residue tank of the filter press I through a pipeline.
2. A method for improving the leaching rate of low-grade scheelite is characterized by comprising the following specific steps:
the method comprises the steps of S1, roasting and deslagging, wherein the raw ore grade is 22-30% of WO 3 in terms of weight percent, the moisture content is 10-15% of WO 3, the raw ore grade enters a roasting furnace for roasting and deslagging, the roasting temperature is 500-750 ℃, the roasting time is 0.5-2 hours, the COD (chemical oxygen demand) after roasting is less than or equal to 500mg/L, and the moisture is not more than 0.1%;
S2, pulping, namely adding water into the roasted mineral powder to carry out pulping, wherein the liquid-solid ratio of the water to the mineral powder is 3-5:1, adding sodium carbonate solid with the content of more than or equal to 98% and a silicon removing agent in the pulping process, and the concentration of sodium carbonate after pulping is 130-220g/L;
s3, splitting by a cyclone, conveying the ore pulp prepared by the step S2 to the cyclone through a pump, enabling the light phase split by the cyclone to enter an autoclave, and enabling the heavy phase to enter a vertical mill;
S4, crushing and activating a vertical mill, wherein heavy phase is crushed and activated in the vertical mill, the ore grinding time is not less than 30min, the passing rate of mineral granularity-60 meshes is more than 95%, and the ore pulp after vertical milling is conveyed to an autoclave through a pump;
S5, pressure boiling and leaching, wherein the light phase split by the cyclone in S3 and the ore pulp after the S4 vertical mill are subjected to pressure boiling and leaching in a pressure boiling kettle, the pressure boiling temperature is controlled to be 185-220 ℃, and the mixture is discharged to a storage tank after heat preservation is carried out for 0.5-2 hours;
s6, carrying out primary solid-liquid separation, wherein ore pulp in the storage tank is conveyed to a filter press I through a pump for solid-liquid separation, and the separated valuable tungsten-containing solution enters a subsequent workshop for treatment;
S7, enriching, namely adding an antifoaming agent into leached residues in the S6, pulping, wherein the pulp concentration is less than or equal to 20% by weight, and the pulp enters a blanket machine for primary enrichment after pulp mixing, and coarse concentrate of the blanket machine enters a suspension machine for secondary enrichment;
And S8, carrying out secondary solid-liquid separation, wherein the concentrate of the suspension machine enters a filter press II for solid-liquid separation, the mineral powder of the filter press II returns to the S2, and the return water is added with a flocculating agent to enter the S7 for leaching residues for size mixing.
3. The method for improving the leaching rate of low-grade scheelite according to claim 2, wherein the silicon removing agent in S2 is one or more of magnesium oxide with the content of more than or equal to 85 percent, industrial aluminum sulfate and industrial aluminum hydroxide with the content of more than or equal to 64.5 percent in percentage by weight, and the adding amount of the silicon removing agent is 3-5 percent of the weight of mineral powder respectively.
4. The method for improving the leaching rate of low-grade scheelite according to claim 3, wherein the content of calcium oxide in the magnesium oxide is lower than 5%.
5. The method for improving the leaching rate of low-grade scheelite according to claim 2, wherein the adding amount of the antifoaming agent in the step S7 is 3 ‱ of the total solution volume.
6. The method for improving the leaching rate of low-grade scheelite according to claim 2, wherein the adding amount of the flocculant in S8 is less than or equal to 70mg/L according to the turbidity of water.
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