CN111663055B

CN111663055B - Extraction of rhenium and radioactive origin187Methods for Os

Info

Publication number: CN111663055B
Application number: CN202010767409.1A
Authority: CN
Inventors: 李超; 赵鸿; 屈文俊; 温宏利; 黄凡; 赵九江; 周利敏; 李欣尉
Original assignee: National Geological Experimental Testing Center china Geological Survey
Current assignee: National Geological Experimental Testing Center china Geological Survey
Priority date: 2020-08-03
Filing date: 2020-08-03
Publication date: 2022-02-22
Anticipated expiration: 2040-08-03
Also published as: CN111663055A

Abstract

The invention discloses a method for extracting rhenium and radioactive origin¹⁸⁷An Os method belongs to the technical field of mineral extraction, and solves the problem that rhenium and radioactive cause cannot be simultaneously recovered in the prior art¹⁸⁷Os, and the recovery process seriously pollutes the environment. The extraction method comprises the following steps: burdening → roasting → water leaching → filtering to obtain liquid phase and solid phase, the solid phase enters the process of acid boiling molybdenum and distilling osmium to obtain volatile osmium tetroxide, and the volatile osmium tetroxide enters the subsequent extraction¹⁸⁷An Os process; the liquid phase contains rhenium and enters a rhenium extraction process. The rhenium extraction process comprises the following steps: ion exchange extraction of rhenium → concentration; → primary crystallization to obtain ammonium rhenate crystal → secondary crystallization to obtain potassium rhenate crystal. The invention realizes that rhenium and rhenium are simultaneously extracted by adopting one process¹⁸⁷Os。

Description

Extraction of rhenium and radioactive origin187Methods for Os

Technical Field

The invention relates to the technical field of mineral extraction, in particular to a national emerging resource rhenium¹⁸⁷The extraction of Os, especially the extraction of rhenium and radioactive cause from molybdenite¹⁸⁷Methods of Os.

Background

Rhenium is one of the rarest metals on earth, is often used on high-performance aircraft engine turbines, and if rhenium is lacked, the performance and the service life of the engine are severely limited, so rhenium is known as a metal for changing the aviation industry and is an emerging source.

The rhenium reserve in China is less than 240 tons, and is a resource which is more precious than rare earth, and high-specification environmental protection thresholds and control conditions are set in China, so that illegal mining is completely avoided.

Osmium (Os) is an element of group viii of the sixth period of the periodic table, one of the platinum group metal members, and is currently known as the most dense metal. Os has 7 isotopes (184, 186, 187, 188, 189, 190, 192). It is generally considered that¹⁸⁷Production of Re by radioactive decay¹⁸⁷The relative ratio of Os, among several other non-radioactive causes of Os isotopes, is constant.¹⁸⁷Os is present in very small amounts in the earth's crust and has a radioactive origin comparable to other natural isotopes of Os¹⁸⁷Os has particular physical properties.

At present, the existing extraction technology can not recover rhenium and radioactive cause at the same time¹⁸⁷Os, and the recovery process seriously pollutes the environment.

Disclosure of Invention

In view of the above analysis, the present invention aims to provide a method for simultaneously extracting rhenium and a radioactive origin¹⁸⁷The method of Os solves the problem that rhenium and radioactive origin can not be recovered by the prior art¹⁸⁷Os, and the recovery process seriously pollutes the environment.

The purpose of the invention is mainly realized by the following technical scheme:

the invention provides a method for extracting rhenium and radioactive origin¹⁸⁷The method for extracting Os adopts molybdenite as an extraction raw material, and comprises the following steps:

step 1: preparing materials;

step 2: roasting;

and step 3: water leaching;

and 4, step 4: filtering to obtain liquid phase and solid phase, boiling the solid phase with acid to obtain volatile osmium tetroxide, and extracting volatile osmium tetroxide¹⁸⁷Os process to obtain¹⁸⁷An Os metal powder; the liquid phase contains rhenium, and rhenium extraction technology is carried out to obtain potassium rhenate crystals;

the rhenium extraction process comprises the following steps:

step a: extracting rhenium by ion exchange to obtain an eluent containing rhenium;

step b: concentrating the eluent;

step c: primary crystallization is carried out to obtain ammonium rhenate crystals;

step d: and (5) performing secondary crystallization to obtain a potassium rhenate crystal.

On the basis of the scheme, the invention is further improved as follows:

further, the step a comprises the following steps: the rhenium-containing liquid phase in the step 4 flows through an ion exchange column, the ion exchange column is washed by NaOH solution firstly, then is washed by deionized water to be neutral, and then is washed by NH₄The SCN solution elutes the rhenium on the column.

Further, the step b comprises the following steps: concentrating the eluate obtained in step a to a rhenium concentration of 50-100 g/l.

Further, the step d comprises the following steps: and d, dissolving the ammonium rhenate crystal obtained in the step c in deionized water, adding a proper amount of potassium chloride solution, and crystallizing to obtain a potassium rhenate crystal.

Further, in the step 2, the thickness of the baked paving material is 10-20 cm.

Further, the calcination time is 1 to 2 hours.

Further, in the step 3, the water leaching comprises primary leaching and secondary leaching.

Further, the primary leaching comprises the steps of: and (3) putting the calcine obtained in the step (2) into water while the calcine is hot, stirring for 2-3 hours, standing, and taking out to obtain a supernatant.

Further, in the step 1, the batching comprises the following steps: and (2) preparing quicklime into plaster by adding water, drying and crushing to obtain slaked lime powder, and uniformly mixing the slaked lime powder and molybdenite powder according to the ratio of 2: 1.

Further, the step c comprises the following steps: and c, placing the concentrated solution obtained in the step b in a refrigerator for cooling, and separating out ammonium rhenate crystals.

Further, the extraction¹⁸⁷The Os process comprises the following steps:

step i: absorbing and concentrating volatile osmium tetroxide to obtain a concentrated solution;

step ii: adding sodium sulfide into the concentrated solution obtained in the step i to obtain an osmium sulfide precipitate;

step iii: melting the osmium sulfide precipitate by using alkali to obtain an osmium sulfide frit;

step iv: dissolving osmium sulfide frit, adding cerium sulfate, and distilling to obtain absorption liquid;

step v: separating the absorption liquid, adding absolute ethyl alcohol into the lower extraction phase, and reducing the osmium tetroxide into osmium dioxide by the ethyl alcohol;

step vi: reduction of osmium dioxide with hydrogen to give¹⁸⁷And (3) Os metal powder.

Further, in the step vi, the reduction of osmium dioxide by hydrogen comprises the following steps:

step A: introducing hydrogen;

and B: heating to 90-110 deg.C, and maintaining the temperature;

and C: heating to 190-;

step D: heating to 390-;

step E: heating to 670 ℃ for heat preservation.

Further, in the step iii, the alkali melting osmium sulfide precipitate comprises the following steps: firstly, adding sodium hydroxide into a crucible, melting and cooling, adding the osmium sulfide precipitate, then adding sodium hydroxide to cover the osmium sulfide precipitate, and then covering with sodium peroxide.

Further, in the step i, a sodium hydroxide solution is adopted to absorb the volatile osmium tetroxide.

Further, the method also comprises the following steps: and extracting molybdenum.

Compared with the prior art, the invention can realize at least one of the following beneficial effects:

1) the extraction method of the invention treats 40 tons of molybdenite annually to extract¹⁸⁷20g of Os and 30 kg of potassium rhenate, and the yield of the target product is high;

2) by selecting specific extraction raw material-molybdenite, rhenium and rhenium are increased¹⁸⁷And (4) the extraction purity of Os. In particular, can be made¹⁸⁷The extraction purity of Os is as high as 99.9%, and the extraction purity of potassium rhenium is as high as 99.99%.

3) No SO is generated in the recovery process₂No pollution to the environment;

4) realizes the simultaneous extraction of rhenium and rhenium by adopting one process¹⁸⁷Os fills the defect that the prior extraction technology in China cannot simultaneously recover rhenium and radioactive cause¹⁸⁷Blanks of Os;

5) the invention has the advantages of simple equipment, easy operation and low investment.

Additional features and advantages of the invention will be set forth in the description which follows, and in part will be obvious from the description, or may be learned by practice of the invention. The objectives and other advantages of the invention will be realized and attained by the structure particularly pointed out in the written description and drawings.

Drawings

The drawings are only for purposes of illustrating particular embodiments and are not to be construed as limiting the invention, wherein like reference numerals are used to designate like parts throughout.

FIG. 1 shows the extraction according to the embodiment of the present invention¹⁸⁷A flow diagram of Os;

FIG. 2 is a schematic diagram of an embodiment of the present inventionTaking rhenium and¹⁸⁷a flow diagram of Os;

FIG. 3 shows the extraction of Mo, Re and Re according to the embodiment of the present invention¹⁸⁷And (3) a flow chart of Os.

Detailed Description

The preferred embodiments of the present invention will now be described in detail with reference to the accompanying drawings, which form a part hereof, and which together with the embodiments of the invention serve to explain the principles of the invention.

Example one

In one embodiment of the present invention, a radioactive cause is provided¹⁸⁷The extraction method of Os, as shown in fig. 1, extracts molybdenum concentrate, specifically molybdenite, because the reduced ore-forming fluid (for example, Mo in six valence and Mo in seven valence is reduced to Mo in four valence) when molybdenite is formed, and Os in four valence can be reduced to Os in three valence and even to Os in 0 valence. The lower the ionic valence, the larger the ionic radius, and the reduction of the positive quaternary state Os not only produces a larger Os ion, but also causes charge imbalance, and Mo cannot be replaced by the same analog. In the formation environment of molybdenite, the positive quaternary state of Os is reduced to lower-valence Os ions with a larger ionic radius, which is the main reason why molybdenite does not contain ordinary Os.

While Re has a lattice similarity to that of Mo, Re can be similarly substituted for the position of Mo when molybdenite is crystallized.¹⁸⁷Production of Re by radioactive decay¹⁸⁷Os, and therefore the molybdenite, contain only radioactive origin¹⁸⁷Os。

In the embodiment, molybdenite is selected as the extraction raw material, so that the yield is improved¹⁸⁷And (4) the extraction purity of Os. In particular, the present invention relates to a method for producing,¹⁸⁷the extraction purity of Os is as high as 99.9%.

Specifically, the extraction method of the embodiment includes the following steps:

step 1: and (4) batching. The quicklime is made into plaster by watering, dried and crushed to 100-200 meshes. The obtained slaked lime powder and the dried molybdenite powder are uniformly mixed according to the ratio of 2: 1. The equipment used includes a pulverizer, a drying device, a mixer, a scale and a container.

Step 2: and (4) roasting. Placing the prepared mixed material in a reflecting furnace, and introducing air for roasting at 650-750 ℃.

The purpose of the calcination step is to oxidize molybdenum, sulfur, rhenium, and osmium in the raw material to a high valence state. In order to prevent the loss of volatile gas generated in the process of high-temperature oxidation of rhenium and osmium and prevent the environmental pollution caused by the generation of a large amount of sulfur dioxide gas, quicklime powder with a certain proportion is doped into the raw materials, and the elements respectively generate calcium molybdate, calcium sulfate, calcium rhenium and calcium osmium in the roasting process and coexist in the roasted product. The main reaction is as follows:

MoS₂+3CaO+9/2O₂＝CaMoO₄+2CaSO₄+Q

at the same time, rhenium and osmium in molybdenite are also oxidized to rhenate and osmate, remaining in the calcine. Sulfur in the ore sample is oxidized into sulfate radical without generating SO₂And the environment is not polluted.

The optimum placement thickness and firing time needs to be determined by pilot plant experimentation. This is because, if the paving material is too thick, the oxidation reaction is insufficient; and if the paving material is too thin, the experiment efficiency is influenced by a small ore sample amount. This step is therefore critical to ensure osmium recovery, and must ensure adequate oxidation of all components in the sample. In the invention, the paving thickness of four square meters at the bottom is controlled to be 10-20cm, the optimal paving thickness is 15cm, and the roasting time is 1-2 hours.

In order to reduce the cost, the equipment used for roasting is a reverberatory furnace. In order to ensure ventilation quantity, the flue part should be provided with an induced draft fan and an air quantity regulating valve.

Considering that about 10 percent of osmium is burnt out in the roasting process, a circulating leaching device or a dust removal device is arranged at a proper part of a flue so as to recover the part of osmium, thereby improving the recovery rate of the osmium.

And step 3: and (5) soaking in water. Because calcium rhenate has high solubility in water, and calcium molybdate and calcium osmate are almost insoluble in water, the aim of separating osmium can be achieved by water immersion. The water leaching includes a primary leach and a secondary leach.

The first leaching is as follows: and putting the roasted product obtained by roasting into a leaching tank filled with 400 liters of water while the roasted product is hot, mechanically or manually stirring for 2-3 hours, standing, and taking out to obtain a first supernatant.

The secondary leaching is as follows: adding 100L water into the leaching tank with the first supernatant liquid, stirring for 1 hr, standing, taking out to obtain a second supernatant liquid, and mixing the second supernatant liquid with the first supernatant liquid.

The combined clear liquid returns to leach the next batch of calcine. Treating the immersion liquid after four batches of calcine, not returning to use, and introducing CO₂Gas (CO generated by neutralizing sulfuric acid solution in the subsequent molybdenum boiling process can be utilized₂) Neutralize Ca (OH) therein₂To a pH of 8-9 to produce CaCO₃White precipitate, and clear, and then the rhenium can be directly separated by an ion exchange column.

The equipment adopted by the water leaching of the embodiment is a rhenium leaching tank, preferably with mechanical stirring, and the number of the rhenium leaching tanks is 2, and the rhenium leaching tanks are alternately used. The size of the immersion tank is 700 multiplied by 1200mm, the capacity is 600 liters, the distance between a liquid outlet and the bottom of the tank is 300mm, and the material of the tank body can be engineering plastics, glass fiber reinforced plastics or iron plates.

And 4, step 4: and (5) filtering. In order to improve the recovery of rhenium, the second leaching is followed by filtration, which is performed by centrifugation to reduce the residual rhenium in the calcine. After filtration, a liquid phase and a solid phase are obtained. The liquid phase enters a rhenium extraction process to obtain a potassium rhenate crystal, and the solid phase enters a molybdenum acid boiling and osmium distillation process.

The rhenium extraction process comprises the following steps:

step a: and (4) extracting rhenium by ion exchange to obtain an eluent containing rhenium.

Step b: the eluate is concentrated.

Step c: and carrying out primary crystallization to obtain ammonium rhenate crystals.

The process for acid cooking of molybdenum and osmium distillation comprises the following specific steps: adding potassium permanganate and water into the wet calcine material after being soaked in rhenium, stirring, adding concentrated sulfuric acid, heating to boil, and keeping the temperature.

Preferably, 75 kg of the wet calcine after rhenium soaking (if the wet calcine is not centrifugally separated, 150 kg of water is contained, 100 kg of water is added into a reaction kettle, 0.8-0.85 kg of potassium permanganate is added, 600 liters of water (the water content of the calcine should be subtracted), the reaction kettle is closed, a stirrer is started, 50 liters (90 kg) of concentrated sulfuric acid is added and heated to boiling, and the mixture is kept for 1-2 hours (the optimal time is determined through tests), so that slurry is obtained.

And (4) adding calcium molybdate in the calcine into the slurry to perform a subsequent molybdenum extraction process. And oxidizing the hexavalent osmium to octavalent to generate volatile osmium tetroxide, and entering an osmium extraction process.

In order to facilitate the osmium tetroxide to enter the osmium absorber, air is always introduced to the liquid level below the liquid level in the reaction kettle by using an air pump while heating and stirring in the cooking process, so that the generated osmium tetroxide gas is carried out and is sent to the osmium absorber through a conduit and is absorbed by a 10% sodium hydroxide solution in an ice bath.

The osmium extraction process comprises the following steps:

step I: absorbing and concentrating the volatile osmium tetroxide to obtain a concentrated solution. And the volatile osmium tetroxide enters an osmium absorber to be absorbed.

It should be noted that, because a large amount of water vapor enters the osmium absorber along with the osmium tetroxide in the distillation process, the absorption liquid volume is increased continuously, the increased absorption liquid is transferred out periodically, and a proper amount of sodium hydroxide is supplemented. The transferred absorption liquid reaches 100 liters, and then is placed in a 200 liter reaction kettle for concentration and distillation. Neutralizing with sulfuric acid, adding proper amount of potassium permanganate, adding 6L sulfuric acid, heating to boil, and maintaining for over 2 hr. And returning residual liquid after reaction to the molybdenum boiling process for continuous utilization. The absorption liquid is distilled and concentrated again after accumulating to a certain amount.

Step II: and (4) adding sodium sulfide into the concentrated solution in the step I to obtain an osmium sulfide precipitate.

And transferring the solution into a beaker, adding sodium sulfite while stirring until the brown yellow solution is removed and is changed into a light purple red, wherein at the moment, the osmium in the solution is changed into 6-valent from 8-valent, and other oxidizing substances in the solution are also reduced. Analytically pure sodium sulfide was added to the solution and stirred to dissolve sufficiently, producing a large amount of blackish black osmium sulfide immediately.

It should be noted that the amount of sodium sulfide added must be excessive to ensure adequate osmium precipitation. Generally, more than 5g of solid sodium sulfide is added per 500 ml of solution containing about 200mg/L osmium.

Heating the beaker in a water bath to enable osmium sulfide to be condensed and sink, taking down and cooling, standing, when the upper solution is clear and transparent, transferring the supernatant, washing and precipitating with water to reduce alkalinity and salt content, standing until the upper solution is clear, transferring the supernatant (standing to fully precipitate residual osmium sulfide), filtering the lower thick slurry on a negative pressure suction filtration system provided with a 0.45 mu m alkali-resistant filter membrane, when the slurry is quickly dried and not cracked, washing twice with distilled water, finally fully pumping until the osmium sulfide filter cake is cracked, transferring the slurry into a small beaker, drying the slurry in an oven at 70-80 ℃, and when the slurry is quickly dried, crushing large blocks to prevent the large blocks from being too hard and difficult to crush after being completely dried. After drying out, weighing.

Step III: and (3) alkali-melting the osmium sulfide precipitate to obtain an osmium sulfide frit. Firstly, adding sodium hydroxide into a crucible, melting and cooling, adding dry osmium sulfide powder, then adding sodium hydroxide to cover the dry osmium sulfide powder, and then covering with sodium peroxide.

Specifically, 6 corundum crucibles of 30 ml were prepared, 2g of each corundum crucible was added, the mixture was put into a muffle furnace and melted at 300 ℃ for bottoming, and after taking out and cooling, 0.4 g of osmium sulfide dry powder was weighed out, and covered with 4g of finely divided sodium hydroxide and 12-15 g of sodium peroxide, and the crucibles were shaken to be fully covered. And (2) placing the corundum crucible in a 50 ml ceramic crucible, covering, placing the corundum crucible in a muffle furnace at the temperature lower than 200 ℃, slowly heating the corundum crucible to 700 ℃ by using a current of 16-18A, keeping the temperature for 10-15 minutes after about one hour, opening a furnace door, taking out the crucible, and standing and cooling to obtain the osmium sulfide frit.

Step IV: and (5) distilling. Dissolving osmium sulfide frit, adding cerium sulfate, and distilling to obtain absorption liquid.

And (3) extracting the clinker, namely putting the cooled corundum crucible containing the osmium sulfide clinker into a 200 ml beaker containing 70 ml of water (or alkaline raffinate), adding a watch glass, taking out the corundum crucible after the osmium sulfide clinker is completely dissolved, and washing the corundum crucible with water to prevent the volume from being too large.

About 250 ml of the extract from each 3 crucibles was transferred to a 1000 ml distillation flask, about 5g of cerium sulfate was added, the opening of the distillation flask was sealed with 1:1 sulfuric acid, and the absorption tube was sealed with distilled water.

The first absorption tube contains 25 ml of re-purified carbon tetrachloride, covered with 2 ml of distilled water.

The second absorption tube is filled with 20ml of 20% sodium hydroxide, and the mouth of the second absorption tube is washed by water to 40 ml. And cooling the primary absorption tube and the secondary absorption tube by using ice water bath.

The outlet of the second absorption pipe is connected to a negative pressure system.

Adding sulfuric acid from an adding funnel at the upper part of the distiller to ensure that the acidity of the distillate is 4-5 mol/L.

It should be noted that the electric jacket is adopted for heating in the distillation process, the temperature adjusting knob is not required to be adjusted too high, the phenomenon that a large amount of steam is generated due to too violent heating, and the negative pressure system cannot be drawn away in time, so that the distillate is sprayed out from the air inlet. After the solution is boiled, most of osmium is distilled off when the absorbed liquid volume increases by 15 to 20 ml. The temperature is adjusted to be low, the solution is kept to be slightly boiled but the absorption volume is slowly increased, the temperature is adjusted to be high after about 1.5 hours of boiling, all residual osmium attached to the wall of the solution which is steamed out later is flushed by water vapor and is brought into the absorption tube until the absorption tube is full, the heating is stopped, and the temperature is reduced for about half an hour under the negative pressure.

Step V: separating the absorption liquid, adding absolute ethyl alcohol into the lower extraction phase (organic phase), and reducing the osmium tetroxide into osmium dioxide by the ethyl alcohol.

And (3) disconnecting a connecting port of the absorption bottle and the distillation flask, transferring the absorption liquid in the first absorption tube into a polytetrafluoroethylene separating funnel, fully washing the absorption tube to prevent the volatilization loss of high-concentration osmium in carbon tetrachloride, merging the washing liquid into the separating funnel, shaking for 2 minutes, after phase separation, putting the lower organic phase into a conical flask filled with 80 ml of high-grade pure absolute ethyl alcohol, and shaking uniformly. And (3) immediately adding 5ml of carbon tetrachloride after the solution in the first absorption tube is transferred out, cleaning the absorption tube, transferring the carbon tetrachloride in the absorption tube into a separating funnel after an organic phase in the separating funnel is discharged, washing a raffinate phase (water phase) for 2 minutes, after phase splitting, putting the organic phase into a conical flask, and then repeatedly washing once again by using 5ml of carbon tetrachloride. After washing the aqueous phase once more with 25 ml of carbon tetrachloride, the organic phase was taken out of the flask and placed in a first absorption tube covered with 2 ml of water as the absorption solution for the next distillation.

The raffinate, which also contained a quantity of osmium (about 1%), was combined in a 1000 ml bottle and sodium hydroxide solids (about 1mol/L NaOH) were added at a rate of 15-20g/400ml, whereupon the osmium in the residual organic phase also went into the aqueous phase, and the solution appeared reddish-brown. The solution can be used as the extract of alkali fusion cake, acid (10 ml of concentrated sulfuric acid) can be supplemented during distillation, the residual organic phase in the raffinate phase is accumulated to a large extent, the raffinate phase can be transferred into a separating funnel, the organic phase is washed by a small amount of 20% NaOH until the alkali liquor is colorless, the organic phase does not contain osmium, and the solution is discarded.

The secondary absorption liquid is brownish red after being used for two times, and is also merged into the raffinate phase to be used as the extracting solution. The absorption tube is replaced by new NaOH solution.

The first-stage absorption liquid obtained by distilling twice is combined in the same conical flask and is covered and placed.

In the distillation operation, due to the handling of high concentration osmium solutions (up to 20-25 g/l), extra care is taken to prevent volatilization loss and contamination of osmium to ensure product recovery and purity.

In particular, the following aspects should be noted:

1. in the process of installation and disassembly, the first-stage absorption liquid is ensured not to be polluted by sodium, cerium, sulfate radical and the like in the distillation flask and the second-stage absorption liquid absolutely. Each time the operation of contacting with sodium hydroxide (alkali fusion, extraction, absorption liquid replacement, etc.) is performed, the hands must be cleaned, and the whole operation environment is ensured not to be polluted by sodium. The glass conduit in the absorption tube is also properly placed after being taken out, so as to prevent dust pollution.

2. The concentration of osmium in the first absorption tube reaches 20-30g/L, and the special smell of relatively concentrated osmium tetroxide can be smelled. Therefore, preparation work is required before disassembly, the operation is quick, after the closed system of the guide pipe is disassembled, the inside and the outside of the guide pipe are slightly cleaned by a small amount of distilled water immediately, the guide pipe is quickly transferred to a separating funnel, residual carbon tetrachloride in the absorption pipe is cleaned by the distilled water and is transferred to the separating funnel together, and the loss of osmium volatilization is prevented.

3. The distillation residual liquid also contains 5-8mg/L osmium, and the osmium should be returned to the second concentration step for use.

4. Since there is no further purification step from this distillation of the concentrated first absorption liquid, the impurities introduced from this operation are carried over into the product, and care is taken to take each detail without contamination.

It is worth noting that the osmium tetroxide in the conical flask is reduced to osmium dioxide by ethanol, the original clear and colorless solution turns into black ink, the conversion speed is related to the temperature, the adding amount of ethanol and the content of osmium, and the reaction can be completed within several hours generally. To allow the reaction to proceed fully, the solution is typically left for three days. After the conversion is completed, the conical bottle cap is opened, the conical bottle cap is placed in a water bath kettle, the conical bottle cap is heated at 80-90 ℃ to volatilize carbon tetrachloride and ethanol, and after the conical bottle cap is completely dried, the osmium dioxide solid in the conical bottle is transferred to a weighing bottle to be weighed.

Step VI: reduction of osmium dioxide with hydrogen to give¹⁸⁷Os metal powder (abbreviated as "osmium powder").

Weighing a special quartz boat, then weighing 1.5-2 g of osmium dioxide, and uniformly paving. The quartz tube is arranged in the center of a quartz tube of the tube furnace, the outlet of the quartz tube is led into an open container filled with 5 percent NaOH solution, and the air inlet is sealed by water. Introducing hydrogen flow and adjusting to an outlet to generate continuous bubbles. The heating current was adjusted to 6A, slowly heated to 100 ℃ for 10 minutes, then increased to 200 ℃ at 10A, then 10 minutes, to 400 ℃ at 12A, then 10 minutes, and then to 650 ℃ at 16A. After 650 ℃ has been reached, the temperature is maintained for 30 minutes, the heating is stopped, and the osmium dioxide is reduced to¹⁸⁷And (3) Os metal powder.

The hydrogen flow is continuously maintained, and meanwhile, the nitrogen path valve is slowly opened to keep a certain nitrogen flow rate, and then the hydrogen valve is closed. After reduction, is ready for¹⁸⁷And gradually cooling the Os metal powder under the protection of nitrogen flow, cooling to 200-300 ℃ after about 30 minutes, disconnecting the outlet of the quartz tube from the guide tube, and extracting the quartz tube from the tube furnace under the condition of maintaining the nitrogen flow.

In order to prevent air from entering the quartz tube due to the gas contraction of the temperature shock, the nitrogen flow should be slightly increased.

When the temperature of the quartz tube is reduced to room temperature, the nitrogen valve is closed, the quartz boat filled with osmium powder is taken out, after weighing, the osmium powder is transferred into a weighing bottle and is packaged according to certain specification requirements. When the glass tube of the product is closed, it must be ensured that the air is not leaked, so that the osmate powder is prevented from being oxidized and volatilized.

The alkali fusion method was adopted for the present example¹⁸⁷Extracted by Os extraction method¹⁸⁷And (3) determining the purity of the Os metal powder, wherein the test process comprises the following steps:

weighing 5mg of the prepared¹⁸⁷The Os metal powder was placed in a NaOH 2g primed zirconium pan and then 15mL of the common Os standard solution was concentrated to 0.5 mL. A small amount of NaOH powder was added for neutralization, and the concentrated ordinary Os standard solution was transferred to a zirconium pot, which was finally covered with 1g of NaOH and 4g of Na₂O₂And (3) heating the solid powder in a muffle furnace at 700 ℃ for 1h by alkali dissolution. After the zirconium pot was cooled, 20ml of 1:1H was added₂SO₄Neutralizing, and adding 0.5g CeSO₄And separating out Os by distillation. Determination by thermal surface ionization mass spectrometry¹⁸⁷Os/¹⁹⁰The value of Os was 1.057 in combination with the normal Os content (300ug/g) and¹⁸⁷abundance of Os¹⁸⁷Os/¹⁸⁸Os is 0.1211, calculated¹⁸⁷The content of the Os metal powder is more than 99.9 percent.

In this embodiment, the molybdenum extraction process includes the following steps:

step i: and (5) filtering.

Step ii: precipitating to remove impurities such as iron, copper, manganese and the like.

Step iii: and (4) extracting molybdenum by ion exchange.

Step iv: and (4) eluting.

Step v: crystallizing to obtain ammonium molybdate.

The process equipment comprises the following steps:

1) two 1000L glass lining reaction kettles (steam heating or electric heating).

The reaction kettle meets the following requirements:

a. temperature controllable (about 100 degree)

b. The device is provided with a feed inlet (wet calcine, concentrated sulfuric acid, water, return immersion liquid and the like), an air inlet hole, an air outlet hole, a temperature measuring hole, a pressure measuring hole, an observation window, a discharge hole and the like;

c. the system needs to be sealed to prevent osmium leakage, but the pressure is not large and is less than 2 meters of water column;

d. stirring fully, wherein dead angles or concentric circles are prevented from being formed due to the fact that materials are thick, and caking and wall sticking caused by insufficient stirring are prevented;

e. the gas outlet guide pipe is lined with glass lining or polytetrafluoroethylene lining, so that osmium tetroxide is prevented from being reduced and adsorbed.

2) Quantitative sample feeding system-metering pump (concentrated sulfuric acid, acidic filtrate, water, etc.), elevated tank.

3) One 200-liter glass lining reaction kettle (heated by steam or electricity) is used for concentrating the osmium absorbing solution.

4) And the osmium absorber is connected in series with two stages, can be made of stainless steel and can observe the liquid level.

5) A cooling bath for ice bath osmium absorber.

6) And the compression air pump is used for conveying air into the reaction kettle, and the required air inflow is adjustable.

7) The filtering and separating device is required to effectively filter viscous slurry and fully wash the viscous slurry, so that the effective recovery of molybdenum is ensured.

8) The discharging material receiving groove is 1400mm × 1400mm × 500mm, the volume is 1000 liters, the discharging material receiving groove is made of engineering plastics or stainless steel, and the lower part of the discharging material receiving groove is provided with a discharging hole.

9) Container, 10 plastic barrels of 200L, for receiving filtrate and washing water.

10) The refrigerator is used for making ice and cooling the osmium absorbing liquid.

Example two

As shown in fig. 2, the rhenium extraction process of example one more specifically includes the following steps:

The rhenium-containing immersion liquid treated by water immersion flows through an ion exchange column at the flow rate of 500 ml/min, rhenium in the immersion liquid is left on the column, and impurities such as calcium, molybdenum and the like flow out along with the immersion liquidAnd (6) discharging the liquid. When rhenium is detectable in the effluent, indicating that the column capacity is full, the loading of the column is stopped. The effluent can be returned to the rhenium leaching process for continuous use. The column was washed with 50 liters of 10% NaOH solution (to remove molybdenum) and then with deionized water to neutral. With 9% NH₄The SCN solution elutes the rhenium on the column. The flow rate of the eluent is as slow as possible, and the specific conditions and the dosage of the eluent need to be determined through experiments.

Step b: the eluate is concentrated. The eluent is loaded in sections, wherein the solution with rhenium concentration higher than 10 g/L is concentrated to the rhenium concentration of 50-100 g/L at about 80 ℃.

Step c: and carrying out primary crystallization to obtain ammonium rhenate crystals. And cooling the concentrated solution in a refrigerator overnight to precipitate ammonium rhenate crystals.

Step d: and (5) performing secondary crystallization to obtain a potassium rhenate crystal. Dissolving the ammonium rhenate crystal in a small amount of deionized water, adding a proper amount of potassium chloride solution, performing secondary crystallization to obtain potassium rhenate crystal, filtering, and drying at low temperature. The eluate with lower rhenium concentration can be returned for further elution.

The ion exchange columns used in this example were 201 strongly basic anion exchange resins, with an exchange capacity for rhenium of 130 g/kg of resin, two ion exchange columns and a high sump volume of 1200 l. Pumping the immersion liquid into the elevated tank by a pump.

EXAMPLE III

As shown in fig. 3, the molybdenum extraction process of the first embodiment more specifically includes the following steps:

step i: separating solid and liquid of the slurry, wherein the main component of the solid phase is CaSO₄(Gypsum Fibrosum), adjusting the liquid phase to neutral (pH about 7) with calcium carbonate, filtering, and performing molybdenum extraction on the filtrate.

It should be noted that after the liquid phase is adjusted to be neutral, the liquid phase must be filtered within four hours, otherwise the dissolved molybdenum can be precipitated in the form of calcium molybdate, and the recovery rate of molybdenum is reduced.

After the reaction is finished, the thick slurry in the kettle is completely put into a receiving tank with the volume of 1000 liters, and is introduced into a centrifuge for solid-liquid separation in times, and the liquid phase is collected. Washing filter residue twice with a small amount of water (the washing degree directly influences the recovery rate of molybdenum), and collecting the water washing liquid separately.

And (4) after the acidity of the direct filtrate is measured, returning the filtrate to the reaction kettle, and continuing to digest the next batch of calcine. The amount of potassium permanganate added was adjusted according to the color of the filtrate, and concentrated sulfuric acid (about 30 liters) was added to a total amount of 50 liters. And so on, the primary filtrate can be repeatedly used to treat more than four batches of calcine. After four batches of calcine are treated, stirring is continued after the reaction is finished, fine calcium carbonate (limestone) powder is slowly added from a feeding port, and the sulfuric acid in the solution is neutralized. At this time, a large amount of CO is produced₂And gas is introduced into the immersion liquid after the rhenium immersion for four times through the gas outlet guide pipe, and calcium hydroxide in the immersion liquid is neutralized. Then, the slurry was put into a receiving tank, the pH was further adjusted to about 7 with calcium carbonate, and the slurry was filtered to give a filtrate having a molybdenum concentration of about 60 g/l, and sent to a molybdenum extraction step.

The collected water washing liquid is used for treating a new batch of calcine after acidity measurement.

Step ii: precipitating to remove impurities such as iron, copper, manganese and the like. And (e) adding NaOH into the filtrate obtained in the step (i), adjusting the pH value to be about 10, adding hydrogen peroxide, standing for 1h, filtering, washing to obtain yellow filtrate, and adding impurities such as iron, copper, manganese and the like into filter residues.

Specifically, the liquid phase after solid-liquid separation is subjected to sulfate radical removal by using calcium carbonate to obtain a filtrate with the pH value of about 7, wherein a large amount of impurity elements, mainly iron, copper, manganese and the like, are removed as much as possible before ion exchange. NaOH (concentrated solution to prevent local excess if large particles) is slowly and uniformly added to the filtrate, stirred to-pH 10, and then a small amount of hydrogen peroxide is added until the purple-red solution turns yellow (the amount added depends on the manganese content in the solution, and is generally 0.5% of the filtrate), indicating that manganese has been reduced to divalent. Standing for one hour to generate a large amount of precipitate, centrifugally filtering, washing the precipitate with water, and discarding filter residues. The removal rate of iron and manganese in the filtrate is 100 percent, and the removal rate of copper is more than 98 percent.

Step iii: and (4) extracting molybdenum by ion exchange. And (3) adjusting the filtrate obtained in the step ii to be acidic, and performing ion exchange.

Adjusting the pH value of the filtrate (pH10) after impurity removal to 2 with nitric acid, supplementing a proper amount of hydrogen peroxide until the solution is bright yellow if the addition amount of hydrogen peroxide is insufficient during impurity removal of the previous precipitate, pouring the solution into an exchange tank filled with 200 kg of macroporous weakly-alkaline anion exchange resin, and intermittently and slowly stirring, wherein after one day, the yellow color of the solution disappears, which indicates that molybdenum in the solution is adsorbed by the resin, (and in order to ensure that the adsorption amount of the resin reaches saturation, the molybdenum-containing solution can be continuously added until the yellow color does not disappear). The exchanged solution is discharged and can be discarded if the molybdenum content is low, and the residual molybdenum is left for batch exchange or is recovered by loading on a column if the molybdenum content is high.

The resin saturated and adsorbed with molybdenum in the exchange tank is firstly washed with slightly acidic water containing a small amount of nitric acid (the washing water can be poured out and put on a column), and then washed with deionized water for several times. The washing efficiency can be improved if the centrifugal separation is carried out.

Step iv: and (4) eluting. And eluting the molybdenum adsorbed by the resin by using a mixed solution of ammonium nitrate and ammonium hydroxide which has the same volume with the resin.

The molybdenum adsorbed by the resin was eluted with a mixed solution of ammonium nitrate and ammonium hydroxide (ammonium nitrate concentration of 1mol/L and ammonium hydroxide concentration of 12.5%) in an equal volume (about 450 liters) to the resin. The mixture was stirred in the exchange tank for 20 minutes, and the eluate was filtered off by centrifugation. The resin was washed with 200 liters of deionized water on a centrifuge and the wash water was collected for formulation of the next batch of eluent. The washed resin was washed with water containing nitric acid to a pH of 2 and was ready for further exchange of molybdenum.

Step v: crystallizing to obtain ammonium molybdate.

The concentration of molybdenum in the eluent obtained by filtration is about 170 g/L, and the eluent can be heated and evaporated in a heating kettle to crystallize and separate out ammonium paramolybdate. Evaporating until ammonium nitrate in the solution is nearly saturated, filtering to separate out ammonium molybdate, and continuously eluting molybdenum in the resin after supplementing ammonium hydroxide into the mother solution. Ammonium tetramolybdate crystals can also be obtained by neutralization after evaporation to a molybdenum concentration of 200 g/l.

The precipitated ammonium molybdate was filtered and dried (<89 ℃ C.) to obtain an ammonium molybdate product.

The equipment required by the molybdenum extraction process is as follows:

1) a precipitation tank for precipitating impurities, wherein the precipitation tank is 1000mm multiplied by 1500mm and can be used for stirring, and a liquid outlet is arranged at the lower part;

2) the exchange tank is used for ion exchange of the molybdenum digestion solution, and the two exchange tanks are alternately used and require the same 1);

3) the resin, D301 macroporous weakly basic anion exchange resin (produced by chemical plant of Tianjin Nankai university) was 200 kg per tank, and 400 kg in total. Washing the new resin with water to remove impurities, soaking in 10% nitric acid, washing, and converting, and selecting with water to weak acidity for use;

4) the centrifugal filter is used for precipitating impurities, washing resin and filtering and separating ammonium molybdate crystals;

5) a drying device for drying the ammonium molybdate product, wherein the temperature is required to be controllable;

6) the evaporation (neutralization) kettle is 500 liters, and the stirring can be heated. It is best to achieve reduced pressure evaporation, if temporary unconditional, then open evaporation. Acid resistance (pH2) is required if neutralization is considered;

7) the ion exchange column is used for recovering low-content molybdenum in the washing liquid, and has the same specification as the ion exchange column for extracting rhenium;

8) and the pump is used for transferring a large amount of liquid.

The extraction method can realize annual treatment of 40 tons of molybdenite and co-extraction of radioactive cause¹⁸⁷20g of Os, 30 kg of potassium rhenate and 30 tons of ammonium molybdate.

The extraction method can realize the full separation of molybdenum and rhenium, and obtain high-purity potassium rhenium and ammonium molybdate. The raw materials used in the recovery process are easily available, and SO is not generated₂The waste gas has little influence on the environment and can recover the radioactive cause¹⁸⁷And (7) Os. In addition, the invention has the advantages of simple equipment, easy operation and low investment.

The above description is only for the preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any changes or substitutions that can be easily conceived by those skilled in the art within the technical scope of the present invention are included in the scope of the present invention.

Claims

1. Extraction of rhenium and radioactive origin¹⁸⁷The Os extraction method is characterized in that the extraction raw material is molybdenite, and the extraction method comprises the following steps:

step 1: preparing materials: preparing quicklime into lime paste by passing water, drying, crushing to 100-mesh and 200-mesh to obtain slaked lime powder, and uniformly mixing the slaked lime powder and the dried molybdenite powder according to the proportion of 2: 1;

step 2: roasting: placing the prepared mixed material in a reflecting furnace, and introducing air for roasting at 650-750 ℃;

and step 3: water leaching;

the rhenium extraction process comprises the following steps:

step b: concentrating the eluent;

2. Extraction of rhenium and a radioactive origin according to claim 1¹⁸⁷The method of Os is characterized in that the step a comprises the following steps: the rhenium-containing liquid phase in the step 4 flows through an ion exchange column, the ion exchange column is washed by NaOH solution firstly, then is washed by deionized water to be neutral, and then is washed by NH₄The SCN solution elutes the rhenium on the column.

3. Extraction of rhenium and a radioactive origin according to claim 1¹⁸⁷The method of Os, characterized in that the step b comprises the following steps: concentrating the eluate obtained in step a to a rhenium concentration of 50-100 g/l.

4. Extraction of rhenium and a radioactive origin according to claim 1¹⁸⁷The method of Os, characterized in that the step d comprises the following steps: c, dissolving the ammonium rhenate crystal obtained in the step c into deionized water, adding a proper amount of potassium chloride solution, and crystallizing to obtain a potassium rhenate crystal。

5. Extraction of rhenium and a radioactive origin according to claim 1¹⁸⁷The Os method is characterized in that in the step 2, the thickness of the roasted paving material is 10-20 cm.

6. Extraction of rhenium and a radioactive origin according to claim 5¹⁸⁷The Os method is characterized in that the roasting time is 1-2 hours.

7. Extraction of rhenium and a radioactive origin according to any one of claims 1 to 6¹⁸⁷The method of Os is characterized in that in the step 3, the water leaching comprises primary leaching and secondary leaching.

8. Extraction of rhenium and a radioactive origin according to claim 7¹⁸⁷Os process, characterized in that the primary leaching comprises the steps of: and (3) putting the calcine obtained in the step (2) into water while the calcine is hot, stirring for 2-3 hours, standing, and taking out to obtain a supernatant.

9. Extraction of rhenium and of a radioactive origin according to any one of claims 1 to 6, 8¹⁸⁷The Os method is characterized by further comprising the following steps: and extracting molybdenum.