CN110551892A - mineral separation device containing tungsten-tin concentrate - Google Patents
mineral separation device containing tungsten-tin concentrate Download PDFInfo
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- CN110551892A CN110551892A CN201910989008.8A CN201910989008A CN110551892A CN 110551892 A CN110551892 A CN 110551892A CN 201910989008 A CN201910989008 A CN 201910989008A CN 110551892 A CN110551892 A CN 110551892A
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- 239000012141 concentrate Substances 0.000 title claims abstract description 84
- AWXLLPFZAKTUCQ-UHFFFAOYSA-N [Sn].[W] Chemical compound [Sn].[W] AWXLLPFZAKTUCQ-UHFFFAOYSA-N 0.000 title claims abstract description 32
- 229910052500 inorganic mineral Inorganic materials 0.000 title claims description 11
- 239000011707 mineral Substances 0.000 title claims description 11
- 238000000926 separation method Methods 0.000 title description 15
- 238000002386 leaching Methods 0.000 claims abstract description 159
- 239000002002 slurry Substances 0.000 claims abstract description 126
- WFKWXMTUELFFGS-UHFFFAOYSA-N tungsten Chemical compound [W] WFKWXMTUELFFGS-UHFFFAOYSA-N 0.000 claims abstract description 72
- 229910052721 tungsten Inorganic materials 0.000 claims abstract description 72
- 239000010937 tungsten Substances 0.000 claims abstract description 72
- ATJFFYVFTNAWJD-UHFFFAOYSA-N Tin Chemical compound [Sn] ATJFFYVFTNAWJD-UHFFFAOYSA-N 0.000 claims abstract description 68
- 238000001704 evaporation Methods 0.000 claims abstract description 65
- 230000008020 evaporation Effects 0.000 claims abstract description 65
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims abstract description 39
- 238000000354 decomposition reaction Methods 0.000 claims abstract description 31
- 238000001914 filtration Methods 0.000 claims abstract description 31
- 239000003513 alkali Substances 0.000 claims abstract description 26
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 18
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 claims abstract description 17
- 239000000706 filtrate Substances 0.000 claims abstract description 13
- 239000007788 liquid Substances 0.000 claims description 43
- 238000002156 mixing Methods 0.000 claims description 43
- 238000001816 cooling Methods 0.000 claims description 40
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 22
- 238000000498 ball milling Methods 0.000 claims description 19
- 238000003756 stirring Methods 0.000 claims description 19
- 238000006243 chemical reaction Methods 0.000 claims description 17
- 239000011268 mixed slurry Substances 0.000 claims description 16
- 238000007701 flash-distillation Methods 0.000 claims description 3
- 230000008676 import Effects 0.000 claims 4
- 238000011084 recovery Methods 0.000 abstract description 9
- 238000000034 method Methods 0.000 description 63
- 230000008569 process Effects 0.000 description 44
- 239000007789 gas Substances 0.000 description 27
- 230000000694 effects Effects 0.000 description 13
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 10
- 238000004519 manufacturing process Methods 0.000 description 9
- 239000000047 product Substances 0.000 description 8
- 238000005265 energy consumption Methods 0.000 description 6
- 239000008235 industrial water Substances 0.000 description 6
- 239000007791 liquid phase Substances 0.000 description 6
- 239000002245 particle Substances 0.000 description 6
- 230000000630 rising effect Effects 0.000 description 5
- 229910000029 sodium carbonate Inorganic materials 0.000 description 5
- 238000004458 analytical method Methods 0.000 description 4
- 230000009286 beneficial effect Effects 0.000 description 4
- 239000000498 cooling water Substances 0.000 description 4
- 238000007599 discharging Methods 0.000 description 4
- 238000005485 electric heating Methods 0.000 description 4
- 238000000227 grinding Methods 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 4
- 150000002500 ions Chemical class 0.000 description 4
- 230000014759 maintenance of location Effects 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- 238000003825 pressing Methods 0.000 description 4
- 238000005086 pumping Methods 0.000 description 4
- 239000007787 solid Substances 0.000 description 4
- 239000002253 acid Substances 0.000 description 3
- 229910052785 arsenic Inorganic materials 0.000 description 3
- RQNWIZPPADIBDY-UHFFFAOYSA-N arsenic atom Chemical compound [As] RQNWIZPPADIBDY-UHFFFAOYSA-N 0.000 description 3
- 238000010924 continuous production Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 238000009834 vaporization Methods 0.000 description 3
- 230000008016 vaporization Effects 0.000 description 3
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- 150000004649 carbonic acid derivatives Chemical class 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- ZXOKVTWPEIAYAB-UHFFFAOYSA-N dioxido(oxo)tungsten Chemical compound [O-][W]([O-])=O ZXOKVTWPEIAYAB-UHFFFAOYSA-N 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Chemical compound [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 description 2
- XOLBLPGZBRYERU-UHFFFAOYSA-N tin dioxide Chemical compound O=[Sn]=O XOLBLPGZBRYERU-UHFFFAOYSA-N 0.000 description 2
- 239000002918 waste heat Substances 0.000 description 2
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 229910052681 coesite Inorganic materials 0.000 description 1
- 229910052906 cristobalite Inorganic materials 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 229910000027 potassium carbonate Inorganic materials 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 229910052682 stishovite Inorganic materials 0.000 description 1
- 229910052905 tridymite Inorganic materials 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 238000001238 wet grinding Methods 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
- C22B25/00—Obtaining tin
- C22B25/04—Obtaining tin by wet 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
- C22B3/04—Extraction of metal compounds from ores or concentrates by wet processes by leaching
- C22B3/12—Extraction of metal compounds from ores or concentrates by wet processes by leaching in inorganic alkaline solutions
-
- 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
-
- 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
-
- 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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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (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)
- Inorganic Chemistry (AREA)
- Manufacture And Refinement Of Metals (AREA)
Abstract
The invention provides a beneficiation device for tungsten-tin-containing concentrate. The device comprises an alkali decomposition unit, a flash evaporation unit and a filtering unit, wherein the alkali decomposition unit is used for carrying out pressure leaching on the tungsten-containing tin concentrate by adopting soluble carbonate or sodium hydroxide as a leaching agent to obtain leached ore pulp; the flash evaporation unit is connected with the alkali decomposition unit and is used for carrying out flash evaporation treatment on the leached ore pulp to obtain concentrated slurry; the filtering unit is connected with the flash evaporation unit and is used for filtering the concentrated slurry to obtain tin concentrate and filtrate. The beneficiation device provided by the invention can improve the quality stability of scheelite prepared from tin concentrate and subsequent filtrate, and the recovery rates of tin and tungsten are high.
Description
Technical Field
The invention relates to the technical field of ore dressing, in particular to an ore dressing device for tungsten-tin-containing concentrate.
Background
The abundance of tungsten in the crust is 1.1 x 10 -6, and tungsten-containing minerals with the highest industrial value and the highest reserves found in the world are wolframite and scheelite, with the exploitation and consumption of high-quality wolframite and high-grade scheelite resources for many years, low-grade scheelite (tungsten-containing tin concentrate) associated with cassiterite gradually enters the research field, and the two are difficult to separate effectively by the prior art.
The existing method for separating and extracting tungsten from tungsten-containing tin concentrate mainly comprises an acid decomposition method, a soluble carbonate sintering-water leaching method and a sodium hydroxide pressure leaching method, and a small number of enterprises apply the soluble carbonate pressure leaching method.
the acid decomposition method can only treat tungsten concentrate with high grade and less impurities basically, but cannot treat tungsten ore with high content of phosphorus and arsenic, and when the acid is used for treating tin concentrate with low content of tungsten, the flow is long, the recovery rate is low, and the economic benefit is not good. The process for treating the tungsten-tin concentrate by the soluble carbonate sintering-water leaching method can realize the high-efficiency separation of tungsten and tin. However, when this method is used to treat tin concentrate containing tungsten, arsenic in the concentrate will enter the leaching solution along with tungsten, which makes the later-stage impurity removal difficult, so this method cannot treat concentrate with high arsenic content. Therefore, enterprises mostly adopt a sodium hydroxide high-pressure leaching method, and a small number of enterprises adopt a soluble carbonate pressure leaching method to carry out ore dressing treatment on the tungsten-containing tin concentrate. However, enterprises adopting the process technology all produce discontinuously, and the product quality cannot be guaranteed.
Disclosure of Invention
The invention mainly aims to provide a beneficiation device for tungsten-containing tin concentrate, which aims to solve the problem of unstable product quality when sodium hydroxide or soluble carbonate is subjected to pressure leaching on the tungsten-containing tin concentrate in the prior art.
In order to achieve the above object, according to one aspect of the present invention, there is provided a beneficiation plant for tungsten-containing tin concentrate, comprising: the alkali decomposition unit is used for carrying out pressure leaching on the tungsten-tin-containing concentrate by adopting soluble carbonate or sodium hydroxide as a leaching agent to obtain leached ore pulp; the flash evaporation unit is connected with the alkali decomposition unit and is used for carrying out flash evaporation treatment on the leached ore pulp to obtain concentrated pulp; and the filtering unit is connected with the flash evaporation unit and is used for filtering the concentrated slurry to obtain tin concentrate and filtrate.
further, the alkali decomposition unit includes: the slurry mixing tank is provided with a leaching agent inlet, a first water inlet, a mineral aggregate inlet and a first slurry outlet and is used for preparing mixed slurry; the pressure leaching kettle is provided with a first slurry inlet and a leached ore pulp outlet, the first slurry inlet is connected with the first slurry outlet through a slurry conveying pipeline, the leached ore pulp outlet is connected with the flash evaporation unit through a leached ore pulp conveying pipeline, and the pressure leaching kettle is used for pressure leaching of mixed slurry.
Further, the size mixing tank is provided with a steam inlet, the flash evaporation unit is provided with a steam outlet, and the steam outlet is connected with the steam inlet through a steam conveying pipeline.
Further, the pressure leaching kettle is also provided with a gas outlet and a condensate inlet; the alkali decomposition unit further comprises a gas-liquid separator, the gas-liquid separator is provided with a gas inlet, a non-condensable gas outlet and a condensate outlet, the gas inlet is connected with the gas outlet, and the condensate outlet is connected with the condensate inlet.
Further, the flash unit comprises: the flash evaporation kettle is provided with a steam outlet, a leached ore pulp inlet and a concentrated slurry outlet, and the leached ore pulp inlet is connected with the leached ore pulp outlet of the pressurized leaching kettle through a leached ore pulp conveying pipeline; and the cooling device is provided with a concentrated slurry inlet and a cooled slurry outlet, the concentrated slurry inlet is connected with the concentrated slurry outlet, and the cooled slurry outlet is connected with the filtering unit through a cooled slurry conveying pipeline.
Furthermore, the ore dressing device also comprises a ball milling unit, the ball milling unit is provided with an abrasive outlet, and the abrasive outlet is connected with the mineral aggregate inlet of the size mixing tank through an abrasive conveying pipeline.
further, the ball milling unit is a wet mill.
Further, the filtering unit is a plate-and-frame filter press.
Further, the pressure leaching kettle is a horizontal reaction vessel with at least one stirring paddle.
Further, the ore dressing device still includes: the first pump body is arranged on the leached ore pulp conveying pipeline; and the second pump body is arranged on the cooling slurry conveying pipeline.
The technical scheme of the invention is applied, and the ore dressing device for the tungsten-containing tin concentrate is provided, and comprises an alkali decomposition unit, a flash evaporation unit and a filtering unit, wherein the alkali decomposition unit is used for carrying out pressure leaching on the tungsten-containing tin concentrate by using soluble carbonate or sodium hydroxide as a leaching agent to obtain leached ore pulp; the flash evaporation unit is connected with the alkali decomposition unit and is used for carrying out continuous flash evaporation treatment on the leached ore pulp to obtain concentrated slurry; the filtering unit is connected with the flash evaporation unit and is used for filtering the concentrated slurry to obtain tin concentrate and filtrate.
The device is adopted to carry out ore dressing on the tungsten-containing tin concentrate, sodium hydroxide or soluble carbonate is utilized to carry out pressure leaching on the tungsten-containing tin concentrate in the alkali decomposition unit, tungsten can be converted into ions to enter a leaching solution, and tin is not leached. The leached ore pulp after leaching can be subjected to flash evaporation through a flash evaporation unit, so that the liquid phase content is reduced, and concentrated slurry is formed. And then, filtering the concentrated slurry through a filtering unit to obtain a filtrate with high tin concentrate and tungsten content. The device utilizes the flash evaporation process, and the flash evaporation process is that the leaching slurry is continuously sprayed into the flash evaporation unit to carry out continuous liquid phase vaporization under the negative pressure condition, so that the effect of continuously discharging steam and concentrated slurry is achieved, the continuous production of pressure leaching, continuous flash evaporation concentration and filtration of tungsten-containing tin concentrate is realized, the tungsten content in the concentrated slurry can be improved through the continuous flash evaporation process, and the separation effect of tin and tungsten is improved. The two reasons are beneficial to ensuring the quality stability of the scheelite prepared from the tin concentrate and the subsequent filtrate, and the recovery rates of tin and tungsten are high.
Drawings
the accompanying drawings, which are incorporated in and constitute a part of this application, illustrate embodiments of the invention and, together with the description, serve to explain the invention and not to limit the invention. In the drawings:
Figure 1 shows a schematic diagram of a beneficiation plant of a tungsten-tin containing concentrate according to one embodiment of the present invention;
Wherein the figures include the following reference numerals:
10. An alkali decomposition unit; 11. a size mixing tank; 12. pressurizing the leaching kettle; 13. a gas-liquid separator; 101. a first pump body; 20. a flash unit; 21. a flash evaporation kettle; 22. a cooling device; 201. a second pump body; 30. a filtration unit; 40. a ball milling unit;
a. tungsten-tin containing concentrate; b. a leaching agent; c. water; d. tin concentrate; e. and (6) filtering the solution.
Detailed Description
It should be noted that the embodiments and features of the embodiments in the present application may be combined with each other without conflict. The present invention will be described in detail below with reference to the embodiments with reference to the attached drawings.
The present application is described in further detail below with reference to specific examples, which should not be construed as limiting the scope of the invention as claimed.
As described in the background section, the prior art pressure leaching of tungsten-tin containing concentrates with sodium hydroxide or soluble carbonates presents the problem of unstable product quality.
In order to solve the problem, the invention provides a beneficiation device for tungsten-containing tin concentrate, as shown in fig. 1, which comprises an alkali decomposition unit 10, a flash evaporation unit 20 and a filtering unit 30, wherein the alkali decomposition unit 10 is used for carrying out pressure leaching on the tungsten-containing tin concentrate by using soluble carbonate or sodium hydroxide as a leaching agent to obtain leached ore pulp; the flash evaporation unit 20 is connected with the alkali decomposition unit 10 and is used for carrying out flash evaporation treatment on the leached ore pulp to obtain concentrated slurry; a filtration unit 30 is connected to the flash unit 20 for filtering the concentrated slurry to obtain tin concentrate and filtrate.
the device is adopted to perform ore dressing on the tungsten-containing tin concentrate, sodium hydroxide or soluble carbonate is utilized to perform pressure leaching on the tungsten-containing tin concentrate in the alkali decomposition unit 10, tungsten can be converted into ions to enter leaching liquid, and tin is not leached. The leached pulp after leaching can be flashed through a flash unit 20 to reduce the liquid phase content and form a concentrated slurry. The concentrated slurry is then filtered through a filtration unit 30 to obtain a tin concentrate and a filtrate with a higher tungsten content. The device utilizes the continuous flash evaporation process, and the flash evaporation process is that the leaching slurry is continuously sprayed into the flash evaporation unit 20 to carry out continuous liquid phase vaporization under the negative pressure condition, so that the effect of continuously discharging steam and concentrated slurry is achieved, the continuous production of pressure leaching, continuous flash evaporation concentration and filtration of the tungsten-containing tin concentrate is realized, the tungsten content in the concentrated slurry can be improved through the continuous flash evaporation process, and the separation effect of tin and tungsten is improved. The two reasons are beneficial to ensuring the quality stability of the scheelite prepared from the tin concentrate and the subsequent filtrate, and the recovery rates of tin and tungsten are high.
In a preferred embodiment, the alkali decomposition unit 10 comprises a size mixing tank 11 and a pressure leaching kettle 12, the size mixing tank 11 is provided with a leaching agent inlet, a first water inlet, a mineral aggregate inlet and a first slurry outlet, and the size mixing tank 11 is used for preparing mixed slurry; the pressure leaching kettle 12 is provided with a first slurry inlet and a leached pulp outlet, the first slurry inlet is connected with the first slurry outlet through a slurry conveying pipeline, the leached pulp outlet is connected with the flash evaporation unit 20 through a leached pulp conveying pipeline, and the pressure leaching kettle 12 is used for pressure leaching of the mixed slurry. The raw materials participating in pressure leaching can be presized by utilizing the size mixing tank 11 to form mixed size with proper solid content, and then the mixed size enters the pressure leaching kettle 12 to carry out pressure leaching reaction.
Preferably, the pressure leaching kettle 12 is also provided with a sewage draining outlet for discharging when the production is stopped or the pressure leaching kettle is overhauled.
during the pressure leaching process, the temperature of the slurry is relatively high, and the steam produced by the leached slurry after the reaction in the flash evaporation unit 20 also has a relatively high temperature. In a preferred embodiment, the size mixing tank 11 is provided with a steam inlet and the flash unit 20 is provided with a steam outlet, which is connected to the steam inlet via a steam transfer line. Thus, the part of the high-temperature steam flashed off can be passed to the size mixing tank 11 to preheat the mixed size. This can effectively recycle the waste heat in the production process, and then reduce the production energy consumption, simultaneously because use continuous leaching and flash distillation technology, can also avoid the energy consumption that brings to the frequent heating and cooling of pressure leaching cauldron 12 in the intermittent production process. Preferably, the leaching agent inlet, the first water inlet, the mineral aggregate inlet and the steam inlet are all arranged at the top of the size mixing tank 11, the first slurry outlet is positioned at the lower part of the size mixing tank 11, and at least one double-layer paddle type stirring paddle is arranged inside the size mixing tank 11.
In addition, due to the high temperature of the slurry in the pressure leaching process, vaporized gas (called slurry steam, which contains part of non-condensable gas) is generated in the pressure leaching process. In a preferred embodiment, the pressure leaching vessel 12 is further provided with a gas outlet and a condensate inlet; the alkali decomposition unit 10 further comprises a gas-liquid separator 13, the gas-liquid separator 13 is provided with a gas inlet, a noncondensable gas outlet and a condensate outlet, the gas inlet is connected with the gas outlet, and the condensate outlet is connected with the condensate inlet. The gas-liquid separator 13 itself is provided with a cooling jacket so that the slurry vapor can be condensed by the gas-liquid separator 13, then subjected to gas-liquid separation, and the condensate separated by the condensation is returned to the pressure leaching tank 12.
It is noted that the above soluble carbonates include, but are not limited to, sodium carbonate and/or potassium carbonate. Preferably, the leaching agent is the soluble carbonate, which has better tin-tungsten separation effect on low-grade tungsten-containing tin concentrate, more than 95% of tungsten can enter the leaching solution in the pressure leaching process, and tin is not leached. Meanwhile, soluble carbonate is used as a leaching agent for leaching ores, only a small amount of carbonate solution is contained in slurry steam discharged in the pressure leaching process, and tail gas can be directly discharged after the solution is recovered through a gas-liquid separator.
Preferably, the first slurry inlet, the leached pulp outlet, the gas outlet and the condensate inlet are all arranged at the top of the pressure leaching kettle 12, and the drain outlet is arranged at the bottom of the pressure leaching kettle 12.
preferably, the cooling jacket of the gas-liquid separator 13 is a water cooling jacket, the gas inlet is located on the side wall of the gas-liquid separator 13, the non-condensable gas outlet is located at the top of the gas-liquid separator 13, and the condensed liquid outlet is located at the bottom of the gas-liquid separator 13.
in a preferred embodiment, the flash evaporation unit 20 comprises a flash evaporation kettle 21 and a cooling device 22, the flash evaporation kettle 21 is provided with a steam outlet, a leached pulp inlet and a concentrated pulp outlet, and the leached pulp inlet and the leached pulp outlet are connected through a leached pulp conveying pipeline; the cooling device 22 is provided with a concentrated slurry inlet and a cooled slurry outlet, the concentrated slurry inlet is connected with the concentrated slurry outlet, and the cooled slurry outlet is connected with the filtering unit 30 through a cooled slurry conveying pipeline. In this way, after the leach slurry has been continuously flashed, it may also be cooled by means of a cooling device 22.
Preferably, the leach pulp inlet is located in the side wall of the flash tank 21, the concentrate outlet is located at the bottom of the flash tank 21, and the steam outlet is located at the top of the flash tank 21.
preferably, the concentrated slurry inlet is disposed at the top of the cooling device 22, the cooled slurry outlet is disposed at the lower portion of the cooling device 22, at least one double-layer paddle type stirring paddle is disposed inside the cooling device 22, and the cooling device 22 is provided with a water cooling jacket.
In a preferred embodiment, the ore dressing device further comprises a ball milling unit 40, wherein the ball milling unit 40 is provided with an abrasive outlet, and the abrasive outlet is connected with the mineral aggregate inlet of the size mixing tank 11 through an abrasive conveying pipeline. In this way, the tungsten-containing tin concentrate can be ground into particles with proper particle size in the ball milling unit 40 in advance, and then enters the size mixing tank 11 for size mixing, so that the effect of pressure leaching can be further improved. Preferably, the ball milling unit 40 is a wet mill. Preferably, the abrasive conveying pipeline is a self-flowing pipeline through which the abrasive flows into the slurry mixing tank 11 under the action of gravity.
The above-mentioned filter unit 30 may be of a conventional type, and preferably, the filter unit 30 is a plate and frame filter press.
Preferably, the pressure leaching tank 12 is a horizontal reaction vessel with at least one stirring blade. The type of the stirring paddle is not limited, and preferably, the stirring paddle is a double-layer paddle type stirring paddle, and the stirring intensity is higher, so that the pressure leaching effect is more favorably improved.
In order to further improve the continuity of the process, the beneficiation plant preferably further comprises a first pump body 101 and a second pump body 201, the first pump body 101 being arranged on the leached pulp delivery line; a second pump body 201 is provided on the cooling slurry delivery line. Both the first pump body 101 and the second pump body 201 are preferably metering pumps.
According to another aspect of the present invention, there is also provided a method for beneficiation of a tungsten-containing tin concentrate, as shown in fig. 1, which includes: adopting soluble carbonate or sodium hydroxide as a leaching agent b, and carrying out pressure leaching on the tungsten-tin-containing concentrate a in an alkali decomposition unit 10 to obtain leached ore pulp; carrying out flash evaporation treatment on the leached ore pulp by using a flash evaporation unit 20 to obtain concentrated slurry; and filtering the concentrated slurry by using a filtering unit 30 to obtain tin concentrate d and filtrate e.
The tungsten-containing tin concentrate is subjected to beneficiation by the method, and is subjected to pressure leaching in the alkali decomposition unit 10 by using sodium hydroxide or soluble carbonate, so that tungsten can be converted into ions to enter a leaching solution, and tin is not leached. The leached pulp after leaching can be subjected to continuous flash evaporation through the flash evaporation unit 20 to reduce the liquid phase content and form concentrated pulp. The concentrated slurry is then filtered through a filtration unit 30 to obtain a tin concentrate and a filtrate with a higher tungsten content. The device utilizes the continuous flash evaporation process, and the flash evaporation process is that the leaching slurry is continuously sprayed into the flash evaporation unit 20 to carry out continuous liquid phase vaporization under the negative pressure condition, so that the effect of continuously discharging steam and concentrated slurry is achieved, the continuous production of pressure leaching, continuous flash evaporation concentration and filtration of the tungsten-containing tin concentrate is realized, the tungsten content in the concentrated slurry can be improved through the continuous flash evaporation process, and the separation effect of tin and tungsten is improved. The two reasons are beneficial to ensuring the quality stability of the artificial scheelite prepared from the tin concentrate and the subsequent filtrate, and the recovery rates of tin and tungsten are high.
in a preferred embodiment, the alkali decomposing element 10 comprises a size mixing tank 11 and a pressure leaching tank 12 arranged in series, and the pressure leaching step comprises: preparing a leaching agent, tungsten-tin-containing concentrate and water into mixed slurry in a slurry mixing tank 11; and (3) carrying out pressure leaching on the mixed slurry in a pressure leaching kettle 12 to obtain leached ore pulp. Thus, the raw materials participating in pressure leaching can be presized by the size mixing tank 11 to form a mixed size with a suitable solid content, and then the mixed size enters the pressure leaching kettle 12 to perform pressure leaching reaction. In the actual operation process, the mixed slurry is continuously fed into the pressure leaching kettle 12 by using the size mixing tank 11 for continuous pressure leaching, and then the generated leaching slurry is continuously fed into the flash evaporation unit 20 for flash evaporation treatment.
The specific process of pressure leaching may be adjusted. Preferably, the leaching pressure in the pressure leaching process is 0.4-2.2 MPa, the leaching temperature is 140-220 ℃, and the leaching time is 1-4 h. Under the process condition, tungsten in the tungsten-containing tin concentrate can be more fully converted into ions to enter the leaching solution, and the tin-tungsten separation effect is better. Preferably, in the pressure leaching process, steam can be used for direct heating, and electric or heat conducting oil can be used for indirect heating.
During the pressure leaching process, the temperature of the slurry is relatively high, and the steam produced by the leached slurry after the reaction in the flash evaporation unit 20 also has a relatively high temperature. In a preferred embodiment, steam is obtained during the continuous flash treatment of the leach pulp using the flash unit 20; the beneficiation process further comprises the step of returning steam to the size mixing tank 11 to preheat the mixed slurry such that the portion of high temperature steam flashed off can be passed to the size mixing tank 11 to preheat the mixed slurry. This can effectively recycle the waste heat in the production process, and then reduce the production energy consumption, simultaneously because use continuous leaching and flash distillation technology, can also avoid the energy consumption that brings to the frequent heating and cooling of pressure leaching cauldron 12 in the intermittent production process. Preferably, the preheating temperature of the mixed slurry is 60-95 ℃.
In a preferred embodiment, slurry vapor is generated simultaneously during the pressure leaching, the alkali decomposition unit 10 further comprises a gas-liquid separator 13, the gas-liquid separator 13 is provided with a cooling jacket, and the beneficiation method further comprises: condensing and gas-liquid separating the high-temperature gas by using a gas-liquid separator 13 to obtain non-condensable gas and condensate; and returning the condensate to the reaction system of the pressure leaching tank 12. Thus, the slurry vapor is condensed by the vapor-liquid separator 13, and then subjected to vapor-liquid separation, and the condensate separated by the condensation is returned to the pressure leaching tank 12.
in a preferred embodiment, the flash unit 20 comprises a flash tank 21 and a cooling device 22 arranged in series; the steps of the continuous flash process include: carrying out continuous flash evaporation treatment on the leached ore pulp by using a flash evaporation kettle 21 to obtain steam and concentrated slurry; the concentrated slurry is cooled using a cooling device 22. In this way, after the leach slurry has been continuously flashed, it may also be cooled by means of a cooling device 22.
Preferably, in the continuous flash evaporation process, the steam is normal pressure steam, and the rising speed of the steam is 0.3-0.8 m/s. This allows for a more rapid concentration.
preferably, in the continuous flash evaporation process, the mass ratio of the steam to the concentrated slurry is 1: 4-6. Thus, on one hand, enough steam can be returned to the size mixing tank 11 for size preheating; on one hand, the solid content of the concentrated slurry can be controlled in a proper range, so that the concentrated slurry has high fluidity to improve the production continuity, and meanwhile, the subsequent filtering process is stable. More preferably, after the flash evaporation treatment in the flash evaporation kettle 21, the temperature of the obtained concentrated slurry is 100-120 ℃, and after the concentrated slurry is cooled by the cooling device 22, the temperature of the concentrated slurry is reduced to 60-80 ℃.
In a preferred embodiment, before the step of preparing the leaching agent, the tungsten-tin-containing concentrate and the water into the mixed slurry in the size mixing tank 11, the beneficiation method further comprises the following steps; the tungsten-tin-containing concentrate is ball-milled by a ball milling unit 40 to obtain an abrasive, and a leaching agent, the abrasive and water are further adopted to prepare a mixed slurry. Thus, as shown in fig. 1, the tungsten-containing tin concentrate a can be ground into particles with a proper particle size in the ball milling unit 40 in advance, and then enters the size mixing tank 11 to be mixed with the leaching agent b and the water c to obtain a mixed slurry, which can further improve the effect of pressure leaching. Preferably, the particle size of the abrasive is 100 to 400 mesh. Of course, the ore type itself having a small particle diameter may not be subjected to the ball milling treatment.
In a preferred embodiment, the ball milling unit 40 is a wet mill, during the ball milling process, the tungsten-tin-containing concentrate a and water c are mixed and then ball milled to obtain the grinding material, and the weight ratio of the tungsten-tin-containing concentrate to the water is 1: 0.5-2.0. Therefore, the tungsten-tin-containing concentrate can be subjected to wet grinding treatment, and the water content in the grinding material is proper.
In a preferred embodiment, the weight ratio of the leaching agent to the abrasive to the water in the process of preparing the mixed slurry is 0.05-0.2: 1: 0.1-1.0. Under the proportion, tungsten in the tungsten-containing tin concentrate can enter the leaching solution more fully, and the tin and tungsten are separated more fully. Meanwhile, the solid content of the slurry is more appropriate, the sufficient fluidity can be ensured to improve the production continuity, and the problems of energy consumption and resource waste caused by overhigh water content can be prevented. More preferably, the process of preparing the mixed slurry is carried out under the condition of stirring, and the stirring time is 10-60 min.
in a preferred embodiment, the filtration unit 30 is a plate and frame filter press.
In a preferred embodiment, the pressure leach tank 12 is a horizontal reaction vessel with at least one paddle.
The beneficial effects of the present invention are further illustrated by the following examples:
Example 1
The beneficiation device shown in figure 1 is adopted to carry out beneficiation treatment on the tungsten-containing tin concentrate. Specifically, the method comprises the following steps:
The main component analysis of the tungsten-tin containing concentrate is as follows:
| Element(s) | Sn | WO3 | Mo | CaO | Fe | S | P | As | SiO2 | MgO |
| the content wt% | 34.75 | 9.54 | 0.40 | 14.92 | 6.39 | 0.33 | 0.04 | 0.68 | 1.89 | 0.25 |
Putting the tungsten-tin-containing concentrate into a ball mill through a screw conveyor at the speed of 500kg/h, and simultaneously adding industrial water into the ball mill at the speed of 250L/h for wet ball milling to prepare an abrasive; the grinding material overflows into a size mixing tank, simultaneously sodium carbonate is added at the feeding speed of 40kg/h, industrial water is added at the speed of 75kg/h, and size mixing is carried out under the stirring state;
The prepared slurry continuously enters a pressure leaching kettle at the flow rate of 865kg/h, and leaching reaction is carried out under the conditions of stirring and electric heating. During the process, the retention time of the slurry in the pressure leaching kettle is 4h, the leaching temperature is 140 ℃, and the leaching pressure is 0.3 MPa. During the leaching reaction, the generated non-condensable gas mixed with part of high-temperature slurry steam (slurry steam) enters a gas-liquid separator, the slurry steam is cooled into liquid through heat exchange with circulating cooling water and flows back to a pressure leaching kettle, and the non-condensable gas is emptied;
And continuously injecting the reacted slurry into a flash evaporation kettle at a flow rate of 865kg/h to continuously generate steam and concentrated slurry while the slurry continuously enters a pressure leaching kettle, wherein the steam is normal-pressure steam, the rising speed is 0.8m/s, and the mass ratio of the steam to the concentrated slurry is 1: 6. The steam returns to the size mixing tank for preheating the ore pulp, and the ore pulp is preheated to 60 ℃. And (3) feeding the concentrated slurry (with the temperature of 100 ℃) into a cooling device at a discharge speed of 740kg/h, cooling to 60 ℃ under the cooling of circulating water, pumping to a plate-and-frame filter press at a speed of 735kg/h, and carrying out filter pressing to obtain a leaching solution and leaching residues, wherein the leaching solution contains tungsten and is sent to subsequent processes to extract tungsten products, and the leaching residues are tin concentrate obtained by separation.
and calculating the yield by stages, wherein the tungsten decomposition rate is stabilized between 95 and 96 percent, and the tin recovery rate is stabilized between 99.6 and 99.9 percent.
Example 2
The beneficiation device shown in figure 1 is adopted to carry out beneficiation treatment on the tungsten-containing tin concentrate. Specifically, the method comprises the following steps:
The specific element analysis of the tungsten-tin-containing concentrate is the same as that of example 1, and the treatment process is as follows:
Putting the tungsten-tin-containing concentrate into a ball mill through a screw conveyor at the speed of 500kg/h, and simultaneously adding industrial water into the ball mill at the speed of 1000L/h for wet ball milling to prepare an abrasive; the grinding material overflows into a size mixing tank, simultaneously sodium carbonate is added at the feeding speed of 300kg/h, industrial water is added at the speed of 150kg/h, and size mixing is carried out under the stirring state;
The prepared slurry continuously enters a pressure leaching kettle at the flow rate of 1950kg/h, and leaching reaction is carried out under the conditions of stirring and electric heating. During the process, the retention time of the slurry in the pressure leaching kettle is 4h, the leaching temperature is 220 ℃, and the leaching pressure is 2.2 MPa. During the leaching reaction, the generated non-condensable gas mixed with part of high-temperature slurry steam (slurry steam) enters a gas-liquid separator, the slurry steam is cooled into liquid through heat exchange with circulating cooling water and flows back to a pressure leaching kettle, and the non-condensable gas is emptied;
While the slurry continuously enters the pressure leaching kettle, the reacted slurry is continuously sprayed into the flash evaporation kettle at the flow rate of 1950kg/h to continuously generate steam and concentrated slurry, the steam is normal-pressure steam, the rising speed is 0.8m/s, and the mass ratio of the steam to the concentrated slurry is 1:4. The steam returns to the size mixing tank for preheating the ore pulp, and the ore pulp is preheated to 95 ℃. And (3) feeding the concentrated slurry (with the temperature of 120 ℃) into a cooling device at a discharge speed of 1560kg/h, cooling to 80 ℃ under the cooling of circulating water, pumping to a plate-and-frame filter press at a speed of 1560kg/h, and carrying out filter pressing to obtain leachate and leaching residues, wherein the leachate contains tungsten and is sent to subsequent processes for extracting tungsten products, and the leaching residues are tin concentrate obtained by separation.
and calculating the yield by stages, wherein the tungsten decomposition rate is stabilized between 96 and 96.5 percent, and the tin recovery rate is stabilized between 99.5 and 99.8 percent.
example 3
The beneficiation device shown in figure 1 is adopted to carry out beneficiation treatment on the tungsten-containing tin concentrate. Specifically, the method comprises the following steps:
The specific element analysis of the tungsten-tin-containing concentrate is the same as that of example 1, and the treatment process is as follows:
Putting the tungsten-tin-containing concentrate into a size mixing tank through a screw conveyor at the speed of 500kg/h, simultaneously adding sodium carbonate at the feeding speed of 25kg/h, adding industrial water at the speed of 350kg/h, and mixing the slurry under the stirring state;
the prepared slurry continuously enters a pressure leaching kettle at the flow rate of 875kg/h, and leaching reaction is carried out under the conditions of stirring and electric heating. During the process, the retention time of the slurry in the pressure leaching kettle is 1h, the leaching temperature is 160 ℃, and the leaching pressure is 0.6 MPa. During the leaching reaction, the generated non-condensable gas mixed with part of high-temperature slurry steam (slurry steam) enters a gas-liquid separator, the slurry steam is cooled into liquid through heat exchange with circulating cooling water and flows back to a pressure leaching kettle, and the non-condensable gas is emptied;
and continuously injecting the reacted slurry into a flash evaporation kettle at a flow rate of 875kg/h while continuously feeding the slurry into a pressure leaching kettle to continuously generate steam and concentrated slurry, wherein the steam is normal-pressure steam, the rising speed is 0.7m/s, and the mass ratio of the steam to the concentrated slurry is 1: 5. The steam returns to the size mixing tank for preheating the ore pulp, and the ore pulp is preheated to 70 ℃. And (2) feeding the concentrated slurry (with the temperature of 110 ℃) into a cooling device at the discharge speed of 730kg/h, cooling to 70 ℃ under the cooling of circulating water, pumping to a plate-and-frame filter press at the speed of 725kg/h, and carrying out filter pressing to obtain leachate and leaching residues, wherein the leachate contains tungsten and is sent to subsequent processes to extract tungsten products, and the leaching residues are tin concentrate obtained by separation.
And calculating the yield by stages, wherein the tungsten decomposition rate is stabilized between 94.8 and 95.6 percent, and the tin recovery rate is stabilized between 99.4 and 99.6 percent.
Example 4
The beneficiation device shown in figure 1 is adopted to carry out beneficiation treatment on the tungsten-containing tin concentrate. Specifically, the method comprises the following steps:
The specific element analysis of the tungsten-tin-containing concentrate is the same as that of example 1, and the treatment process is as follows:
putting the tungsten-tin-containing concentrate into a size mixing tank through a screw conveyor at the speed of 500kg/h, simultaneously adding sodium carbonate at the feeding speed of 50kg/h, adding industrial water at the speed of 500kg/h, and mixing the slurry under the stirring state;
The prepared slurry continuously enters a pressure leaching kettle at the flow rate of 1050kg/h, and leaching reaction is carried out under the conditions of stirring and electric heating. During the process, the retention time of the slurry in the pressure leaching kettle is 0.5h, the leaching temperature is 180 ℃, and the leaching pressure is 0.9 MPa. During the leaching reaction, the generated non-condensable gas mixed with part of high-temperature slurry steam (slurry steam) enters a gas-liquid separator, the slurry steam is cooled into liquid through heat exchange with circulating cooling water and flows back to a pressure leaching kettle, and the non-condensable gas is emptied;
and continuously injecting the reacted slurry into a flash evaporation kettle at a flow rate of 1050kg/h to continuously generate steam and concentrated slurry while the slurry continuously enters a pressure leaching kettle, wherein the steam is normal-pressure steam, the rising speed is 0.6m/s, and the mass ratio of the steam to the concentrated slurry is 1: 4.5. The steam returns to the size mixing tank for preheating the ore pulp, and the ore pulp is preheated to 90 ℃. And (3) feeding the concentrated slurry (with the temperature of 113 ℃) into a cooling device at a discharge speed of 860kg/h, cooling to 80 ℃ under the cooling of circulating water, pumping to a plate-and-frame filter press at a speed of 855kg/h for filter pressing to obtain leachate and leaching residues, wherein the leachate contains tungsten, and the leachate is sent to a subsequent process for extracting tungsten products, and the leaching residues are tin concentrate obtained by separation.
the yield is calculated by stages, the tungsten decomposition rate is stabilized between 95.0 and 95.9 percent, and the tin recovery rate is stabilized between 99.4 and 99.5 percent.
From the above description, it can be seen that the above-described embodiments of the present invention achieve the following technical effects:
more preferably, the ore dressing device for the tungsten-tin-containing concentrate comprises the steps of wet ball milling, size mixing, pressure leaching, flash evaporation and filtering of the tungsten-tin-containing concentrate in sequence, and further comprises the step of condensing part of condensable gas discharged from the pressure leaching kettle in a gas-liquid separator to return to the pressure leaching kettle in the pressure leaching process, and the step of returning steam generated in the flash evaporation process to the size mixing tank for preheating ore pulp. Therefore, the beneficiation effect of the tungsten-tin-containing concentrate is further improved, the tungsten-tin separation is more thorough, the energy consumption is low, the yield is flexible and controllable, meanwhile, the raw material adaptability is wider, and the tungsten-tin-containing concentrate with low grade and high impurity content can be processed.
in addition, the beneficiation device for the tungsten-containing tin concentrate provided by the invention has long service life, and except that the nozzle of the flash evaporation unit is a consumable product and needs to be maintained and replaced regularly, the other devices have stable operation conditions and are not easy to damage.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. The utility model provides a mineral processing device of tungsten-containing tin concentrate which characterized in that includes:
The alkali decomposition unit (10) is used for carrying out pressure leaching on the tungsten-tin-containing concentrate by adopting soluble carbonate or sodium hydroxide as a leaching agent to obtain leached ore pulp;
The flash evaporation unit (20), the flash evaporation unit (20) is connected with the alkali decomposition unit (10) and is used for carrying out flash evaporation treatment on the leached ore pulp to obtain concentrated slurry; and
And the filtering unit (30) is connected with the flash evaporation unit (20) and is used for filtering the concentrated slurry to obtain tin concentrate and filtrate.
2. The beneficiation plant according to claim 1, wherein the alkali decomposition unit (10) comprises:
The slurry mixing tank (11) is provided with a leaching agent inlet, a first water inlet, a mineral aggregate inlet and a first slurry outlet, and the slurry mixing tank (11) is used for preparing mixed slurry;
Pressure leaching kettle (12), pressure leaching kettle (12) are provided with first thick liquids import and leach the ore pulp export, first thick liquids import with first thick liquids export links to each other through thick liquids conveying pipeline, leach the ore pulp export with flash distillation unit (20) link to each other through leaching the ore pulp conveying pipeline, pressure leaching kettle (12) are used for right mixed thick liquids carry out the pressure leaching.
3. The beneficiation plant according to claim 2, wherein the size mixing tank (11) is provided with a steam inlet, and the flash unit (20) is provided with a steam outlet, and the steam outlet is connected with the steam inlet through a steam delivery line.
4. the beneficiation plant according to claim 2, wherein the pressure leaching vessel (12) is further provided with a gas outlet and a condensate inlet; the alkali decomposition unit (10) further comprises a gas-liquid separator (13), wherein the gas-liquid separator (13) is provided with a gas inlet, a non-condensable gas outlet and a condensate outlet, the gas inlet is connected with the gas outlet, and the condensate outlet is connected with the condensate inlet.
5. A beneficiation plant according to claim 3, wherein the flash unit (20) comprises:
The flash evaporation kettle (21) is provided with the steam outlet, a leached ore pulp inlet and a concentrated slurry outlet, and the leached ore pulp inlet is connected with the leached ore pulp outlet of the pressure leaching kettle (12) through the leached ore pulp conveying pipeline;
The cooling device (22), cooling device (22) are provided with concentrated thick liquid import and cooling thick liquid export, concentrated thick liquid import with concentrated thick liquid export links to each other, cooling thick liquid export with filter unit (30) link to each other through cooling thick liquid conveying pipeline.
6. the beneficiation plant according to any one of claims 2 to 5, further comprising a ball milling unit (40), the ball milling unit (40) being provided with an abrasive outlet connected to the mineral aggregate inlet of the dressing trough (11) by an abrasive conveying line.
7. The beneficiation plant according to claim 6, wherein the ball milling unit (40) is a wet mill.
8. Beneficiation plant according to any of claims 1 to 5, wherein the filtration unit (30) is a plate and frame filter press.
9. The beneficiation plant according to any one of claims 2 to 5, wherein the pressure leaching tank (12) is a horizontal reaction vessel with at least one stirring paddle.
10. The beneficiation plant according to claim 5, further comprising:
A first pump body (101), said first pump body (101) being arranged on said leach pulp delivery line; and
A second pump body (201), the second pump body (201) is arranged on the cooling slurry conveying pipeline.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115478175A (en) * | 2022-08-29 | 2022-12-16 | 金川集团股份有限公司 | Pressurized kettle discharge equipment and method thereof |
| WO2023275427A1 (en) * | 2021-07-01 | 2023-01-05 | Metso Outotec Finland Oy | Arrangement and method for air-induced evaporation and cooling |
Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102649995A (en) * | 2012-05-24 | 2012-08-29 | 崇义章源钨业股份有限公司 | Method for transforming wolframite into scheelite |
| CN103484671A (en) * | 2013-08-25 | 2014-01-01 | 云南锡业集团有限责任公司研究设计院 | Method for separating tungsten and tin from tungsten/tin-containing concentrate |
| CN103523800A (en) * | 2013-09-24 | 2014-01-22 | 中国有色集团（广西）平桂飞碟股份有限公司 | Method for recovering excess sodium hydroxide in tungsten smelting crude sodium tungstate solution |
| FI20135118A (en) * | 2013-02-08 | 2014-08-09 | Outotec Oyj | Method and Arrangement for Reducing Autoflash and Slurry Migration in Autoclave Flash Systems |
| CN104789772A (en) * | 2015-04-06 | 2015-07-22 | 桂林理工大学 | Energy-saving and consumption-reducing method for alkaline leaching of scheelite |
| CN106399723A (en) * | 2016-10-17 | 2017-02-15 | 中国恩菲工程技术有限公司 | Processing method of tungsten-containing tin concentrate |
| CN106929668A (en) * | 2017-03-29 | 2017-07-07 | 中国恩菲工程技术有限公司 | It is a kind of to improve the method that lateritic nickel ore high pressure leaches the mesohigh kettle feed pump check valve life-span |
| CN107099679A (en) * | 2017-03-10 | 2017-08-29 | 中国恩菲工程技术有限公司 | Suppress the method that aluminium is leached in lateritic nickel ore high pressure extract technology |
| CN211036040U (en) * | 2019-10-17 | 2020-07-17 | 中国恩菲工程技术有限公司 | Mineral separation device containing tungsten-tin concentrate |
-
2019
- 2019-10-17 CN CN201910989008.8A patent/CN110551892A/en active Pending
Patent Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102649995A (en) * | 2012-05-24 | 2012-08-29 | 崇义章源钨业股份有限公司 | Method for transforming wolframite into scheelite |
| FI20135118A (en) * | 2013-02-08 | 2014-08-09 | Outotec Oyj | Method and Arrangement for Reducing Autoflash and Slurry Migration in Autoclave Flash Systems |
| CN103484671A (en) * | 2013-08-25 | 2014-01-01 | 云南锡业集团有限责任公司研究设计院 | Method for separating tungsten and tin from tungsten/tin-containing concentrate |
| CN103523800A (en) * | 2013-09-24 | 2014-01-22 | 中国有色集团（广西）平桂飞碟股份有限公司 | Method for recovering excess sodium hydroxide in tungsten smelting crude sodium tungstate solution |
| CN104789772A (en) * | 2015-04-06 | 2015-07-22 | 桂林理工大学 | Energy-saving and consumption-reducing method for alkaline leaching of scheelite |
| CN106399723A (en) * | 2016-10-17 | 2017-02-15 | 中国恩菲工程技术有限公司 | Processing method of tungsten-containing tin concentrate |
| CN107099679A (en) * | 2017-03-10 | 2017-08-29 | 中国恩菲工程技术有限公司 | Suppress the method that aluminium is leached in lateritic nickel ore high pressure extract technology |
| CN106929668A (en) * | 2017-03-29 | 2017-07-07 | 中国恩菲工程技术有限公司 | It is a kind of to improve the method that lateritic nickel ore high pressure leaches the mesohigh kettle feed pump check valve life-span |
| CN211036040U (en) * | 2019-10-17 | 2020-07-17 | 中国恩菲工程技术有限公司 | Mineral separation device containing tungsten-tin concentrate |
Non-Patent Citations (1)
| Title |
|---|
| 王吉坤等: "《铜阳极泥现代综合利用技术》", 冶金工业出版社, pages: 212 * |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2023275427A1 (en) * | 2021-07-01 | 2023-01-05 | Metso Outotec Finland Oy | Arrangement and method for air-induced evaporation and cooling |
| CN115478175A (en) * | 2022-08-29 | 2022-12-16 | 金川集团股份有限公司 | Pressurized kettle discharge equipment and method thereof |
| CN115478175B (en) * | 2022-08-29 | 2023-11-21 | 金川集团股份有限公司 | Pressurized kettle discharging equipment and method thereof |
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