Device for reducing ammonia consumption in molybdenum calcine ammonia leaching process
By designing a device including an ammonia water storage tank, a two-stage spray tower and a tandem ammonia immersion reactor, the problems of large ammonia consumption and serious escape in the traditional ammonium molybdate production process are solved, and the efficient utilization of ammonia and environmental protection are achieved.
Patent Information
- Application Number
- CN202420775368.4
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2024-04-15
- Publication Date
- 2025-03-25
- Estimated Expiration
- 2034-04-15
AI Technical Summary
During the traditional ammonium molybdate production process, the ammonia consumption is large during the ammonia immersion process, which causes serious ammonia escape, polluting the environment and endangering the safety of operators.
A device including an ammonia water storage tank, a two-stage spray tower and a series of ammonia immersion reactor is designed. The ammonia consumption is maximized and recycled through the series connection between the first ammonia immersion reactor and the second ammonia immersion reactor and the cleaning and recycling of the two-stage spray tower.
It effectively reduces ammonia consumption, reduces ammonia escape and environmental pollution, and improves the utilization rate of ammonia and protects the safety of operators.
Smart Images
Figure CN222665955U_ABST
Abstract
Description
Technical Field
[0001] The utility model belongs to the technical field of molybdenum roasted sand ammonia leaching equipment, and in particular relates to a device for reducing ammonia consumption in a molybdenum roasted sand ammonia leaching process. Background Art
[0002] Ammonium molybdate is widely used in the production of catalysts, high-purity molybdenum powder, molybdenum products, etc. Molybdenum roasted sand is the raw material for the preparation of ammonium molybdate, mainly MoO3, and also contains some ammonia insoluble substances, such as silicate, MoO2, MoS2, calcium molybdate and other impurities. During the ammonia leaching process, MoO3 reacts with ammonia water to generate (NH4)2MoO4 and enters the solution: MoO3+2NH4OH=(NH4)2MoO4+H2O.
[0003] In the traditional ammonium molybdate production process, the ammonia leaching process is to add water to the reactor, pass ammonia, and then add molybdenum roasted sand. During the feeding process, ammonia gas escapes from the feeding port, which strongly irritates the operator's mouth and nose, making it impossible to open their eyes or even suffocate. The temperature is 70-80°C, and stirring is continued until the pH value reaches 8.5-9.0. In order to increase the leaching rate, a large amount of NH3 is used, and the amount is 120-140% of the theoretical value. (Xiang Tiegen. Molybdenum Metallurgy (M). Central South University Press: pp. 87, 89-90). The use of an open ammonia leaching reactor at normal pressure causes more ammonia to escape. The ammonia leaching process releases a large amount of irritating ammonia gas, which seriously pollutes the environment and is easy to overflow, endangering the safety and health of operators. Utility Model Content
[0004] The utility model aims to provide a device for reducing ammonia consumption in ammonia leaching process of molybdenum roasted sand, thereby solving the problem that ammonia consumption in ammonia leaching process in traditional ammonium molybdate production process is large, resulting in more ammonia escape.
[0005] The technical scheme adopted by the utility model is a device for reducing ammonia consumption in ammonia leaching process of molybdenum roasted sand, comprising an ammonia water storage tank, the ammonia water storage tank is connected to a first high-level tank through a first pipeline, the first high-level tank is connected to a first ammonia leaching reactor through a second pipeline, the first ammonia leaching reactor is connected to a first feed pipe and a second feed pipe, the first ammonia leaching reactor is connected to a second high-level tank through a first tail gas pipe, the second high-level tank is connected to the first pipeline through a third pipeline, the second high-level tank is connected to a second ammonia leaching reactor through a fourth pipeline, the second ammonia leaching reactor is connected to a third feed pipe and a fourth feed pipe, the second ammonia leaching reactor is connected to a two-stage spray tower through a second tail gas pipe, the two-stage spray tower is connected to a pure water inlet pipe, and the two-stage spray tower is connected to the second high-level tank through an ammonia solution outlet pipe.
[0006] The utility model is also characterized in that:
[0007] A first stirring rod is arranged in the first ammonia leaching reactor.
[0008] A second stirring rod is arranged in the second ammonia leaching reactor.
[0009] A valve is arranged on the first pipeline.
[0010] The first tail gas pipe is provided with a first hydraulic jet pump.
[0011] The second tail gas pipe is provided with a second hydraulic jet pump.
[0012] A third hydraulic jet pump is arranged on the ammonia solution outlet pipe.
[0013] The beneficial effects of the utility model are:
[0014] The utility model provides a device for reducing ammonia consumption in ammonia leaching process of molybdenum roasted sand, which avoids large ammonia consumption through series connection of a first ammonia leaching reactor and a second ammonia leaching reactor and cleaning and recycling of a two-stage spray tower, thereby avoiding pollution of the environment by escaping ammonia and simultaneously avoiding harm of ammonia to operators, and is conducive to clean production of ammonium molybdate. BRIEF DESCRIPTION OF THE DRAWINGS
[0015] Figure 1 The utility model is a schematic diagram of the structure of a device for reducing ammonia consumption in ammonia leaching process of molybdenum roasted sand.
[0016] In the figure, 1. ammonia water storage tank, 2. first high-level tank, 3. first feed pipe, 4. second feed pipe, 5. first stirring rod, 6. first ammonia leaching reactor, 7. first tail gas pipe, 8. second high-level tank, 9. third feed pipe, 10. fourth feed pipe, 11. second ammonia leaching reactor, 12. second stirring rod, 13. second tail gas pipe, 14. two-stage spray tower, 15. pure water inlet pipe, 16. ammonia solution outlet pipe, 17. valve, 18. first hydraulic jet pump, 19. second hydraulic jet pump, 20. third hydraulic jet pump, 21. first pipeline, 22. second pipeline, 23. third pipeline, 24. fourth pipeline. DETAILED DESCRIPTION
[0017] The utility model is described in detail below with reference to the accompanying drawings and specific implementation modes.
[0018] The utility model provides a device for reducing ammonia consumption in ammonia leaching process of molybdenum roasted sand, such as Figure 1As shown, it includes an ammonia water storage tank 1, the ammonia water storage tank 1 is connected to a first high-level tank 2 through a first pipeline 21, the first high-level tank 2 is connected to a first ammonia leaching reactor 6 through a second pipeline 22, the first ammonia leaching reactor 6 is connected to a first feeding pipe 3 and a second feeding pipe 4, so as to add reactants to the first ammonia leaching reactor 6 through the first feeding pipe 3 and the second feeding pipe 4, the first ammonia leaching reactor 6 is connected to a second high-level tank 8 through a first tail gas pipe 7, the second high-level tank 8 is connected to the first pipeline 21 through a third pipeline 23, the second high-level tank 8 is connected to a second ammonia leaching reactor 11 through a fourth pipeline 24, the second ammonia leaching reactor 11 is connected to a third feeding pipe 9 and a fourth feeding pipe 10, so as to add reactants to the second ammonia leaching reactor 11 through the third feeding pipe 9 and the fourth feeding pipe 10, the second ammonia leaching reactor 11 is connected to a second tail gas pipe 1 3 is connected to a two-stage spray tower 14, and a pure water inlet pipe 15 is connected to the two-stage spray tower 14, and the pure water inlet pipe 15 provides pure water for the two-stage spray tower 14. The two-stage spray tower 14 is connected to the second high-level tank 8 through an ammonia solution outlet pipe 16 to form a cycle to consume ammonia to the maximum extent; a first stirring rod 5 is provided in the first ammonia leaching reactor 6 to facilitate stirring the reactants in the first ammonia leaching reactor 6; a second stirring rod 12 is provided in the second ammonia leaching reactor 11 to facilitate stirring the reactants in the second ammonia leaching reactor 11; a valve 17 is provided on the first pipeline 21 to facilitate controlling the amount of material transported to the first high-level tank 2 and the second high-level tank 8; a first hydraulic jet pump 18 is provided on the first tail gas pipe 7; a second hydraulic jet pump 19 is provided on the second tail gas pipe 13; and a third hydraulic jet pump 20 is provided on the ammonia solution outlet pipe 16.
[0019] The utility model provides a device for reducing ammonia consumption in ammonia leaching process of molybdenum roasted sand, and its working principle is: hydrogen peroxide and molybdenum roasted sand are added to a first ammonia leaching reactor 6 from a first feeding pipe 3 and a second feeding pipe 4 respectively, hydrogen peroxide and molybdenum roasted sand are added to a second ammonia leaching reactor 11 from a third feeding pipe 9 and a fourth feeding pipe 10 respectively, then a first hydraulic jet pump 18 is turned on, ammonia is dripped into the first ammonia leaching reactor 6 through an ammonia storage tank 1, a first pipeline 21, a first high-level tank 2 and a second pipeline 22, ammonia is dripped into the second ammonia leaching reactor 8 through a fourth pipeline 24, a second high-level tank 8 and a third pipeline 23, and a second hydraulic jet pump 19 is turned on. Water is supplied to the two-stage spray tower 14 through the pure water inlet pipe 15 and the two-stage spray tower 14 is turned on, and the third hydraulic jet pump 20 is turned on. The first ammonia leaching reactor 6 and the second ammonia leaching reactor 11 are connected in series in a closed negative pressure manner through the first tail gas pipe 7. Ammonia escaping from the first ammonia leaching reactor 6 under pressure enters the first ammonia leaching reactor 11 through the first tail gas pipe 7 to continue to dissolve molybdenum roasted sand in ammonia, thereby minimizing the escape of ammonia. The unconsumed ammonia in the second ammonia leaching reactor 11 is absorbed by the two-stage spray tower 14 and then transported to the second high-level tank 8 through the ammonia solution transporting pipe 16 for recycling, thereby improving the utilization rate of ammonia and effectively controlling the unorganized emission of ammonia.
[0020] Example 1
[0021] The device for reducing ammonia consumption in the process of ammonia leaching of molybdenum roasted sand proposed in this embodiment is as follows: Figure 1 As shown, 105 ml of hydrogen peroxide is added to the first ammonia leaching reactor 6 from the first feed pipe 3, 100 g of molybdenum roasted sand with a Mo mass fraction of 59.6% is added to the first ammonia leaching reactor 6 from the second feed pipe 4, and a first stirring rod 5 is used to stir to form a slurry, and the slurry temperature is controlled at 50-55° C., 105 ml of hydrogen peroxide is added to the second ammonia leaching reactor 11 from the third feed pipe 9, and 100 g of molybdenum roasted sand with a Mo mass fraction of 59.6% is added to the second ammonia leaching reactor 11 from the fourth feed pipe 10, and a second stirring rod 12 is used to stir to form a slurry, and the slurry temperature is controlled at 50-55° C. The first hydraulic jet pump 18 is turned on, and 100 ml of ammonia water with a mass fraction of 25% is dripped into the first ammonia leaching reactor 6 through the ammonia water storage tank 1, the first pipeline 21, the first high-level tank 2 and the second pipeline 22, and the fourth pipeline 24, the second high-level tank 8 and the second high-level tank 9 are connected to the first ammonia leaching reactor 6. The third pipeline 23 drips 100 ml of ammonia water with a mass fraction of 25% into the second ammonia leaching reactor 8. When the slurry temperature exceeds 55°C, the dripping is stopped, and when the temperature is lower than 50°C, the dripping is continued until the addition is completed. The second hydraulic jet pump 19 is turned on, and water is supplied to the two-stage spray tower 14 through the pure water inlet pipe 15 and the two-stage spray tower 14 is turned on. The third hydraulic jet pump 20 is turned on. The first ammonia leaching reactor 6 and the second ammonia leaching reactor 11 are connected in series through the first tail gas pipe 7 in a closed negative pressure manner. The ammonia escaping from the first ammonia leaching reactor 6 under pressure enters the first ammonia leaching reactor 11 through the first tail gas pipe 7 to continue to dissolve the molybdenum roasted sand with ammonia, thereby minimizing the escape of ammonia. The unconsumed ammonia in the second ammonia leaching reactor 11 is absorbed by the two-stage spray tower 14, and then transported to the second high-level tank 8 through the ammonia solution transporting pipe 16 for recycling, thereby improving the utilization rate of ammonia and effectively controlling the unorganized emission of ammonia. Finally, 200 ml of ammonia leaching solution was obtained, Mo239.9 g / L, NH3 dosage was 106% of the theoretical value, and the primary leaching rate = 239.9 g / L*0.2 L / 100*59.6% = 80.5%.
[0022] Example 2
[0023] The device for reducing ammonia consumption in the process of ammonia leaching of molybdenum roasted sand proposed in this embodiment is as follows: Figure 1As shown, 110 ml of hydrogen peroxide is added to the first ammonia leaching reactor 6 from the first feed pipe 3, 100 g of molybdenum roasted sand with a Mo mass fraction of 58.26% is added to the first ammonia leaching reactor 6 from the second feed pipe 4, and a first stirring rod 5 is used to stir to form a slurry, and the slurry temperature is controlled at 50-55° C., 110 ml of hydrogen peroxide is added to the second ammonia leaching reactor 11 from the third feed pipe 9, and 100 g of molybdenum roasted sand with a Mo mass fraction of 58.86% is added to the second ammonia leaching reactor 11 from the fourth feed pipe 10, and a second stirring rod 12 is used to stir to form a slurry, and the slurry temperature is controlled at 50-55° C. The first hydraulic jet pump 18 is turned on, and 95 ml of ammonia water with a mass fraction of 28% is dripped into the first ammonia leaching reactor 6 through the ammonia water storage tank 1, the first pipeline 21, the first high-level tank 2 and the second pipeline 22, and a second ammonia water is added to the first ammonia leaching reactor 6 through the fourth pipeline 24, the second high-level tank 8 95 ml of ammonia water with a mass fraction of 28% is added to the second ammonia leaching reactor 8 through the third pipeline 23. When the slurry temperature exceeds 55°C, the addition is stopped, and when the temperature is lower than 50°C, the addition is continued until it is finished. The second hydraulic jet pump 19 is turned on, and water is supplied to the two-stage spray tower 14 through the pure water inlet pipe 15 and the two-stage spray tower 14 is turned on. The third hydraulic jet pump 20 is turned on. The first ammonia leaching reactor 6 and the second ammonia leaching reactor 11 are connected in series through the first tail gas pipe 7 in a closed negative pressure manner. The ammonia escaping from the first ammonia leaching reactor 6 under pressure enters the first ammonia leaching reactor 11 through the first tail gas pipe 7 to continue to dissolve the molybdenum roasted sand in ammonia, thereby minimizing the escape of ammonia. The unconsumed ammonia in the second ammonia leaching reactor 11 is absorbed by the two-stage spray tower 14, and then transported to the second high-level tank 8 through the ammonia solution transporting pipe 16 for recycling, thereby improving the utilization rate of ammonia and effectively controlling the unorganized emission of ammonia. Finally, 200 ml of ammonia leaching solution was obtained, Mo235.6 g / L, NH3 dosage was 115% of the theoretical value, and the primary leaching rate = 235.6 g / L*0.2 L / 100*58.86% = 80.1%.
[0024] Example 3
[0025] The device for reducing ammonia consumption in the process of ammonia leaching of molybdenum roasted sand proposed in this embodiment is as follows: Figure 1As shown, 70 ml of hydrogen peroxide is added to the first ammonia leaching reactor 6 from the first feed pipe 3, 100 g of molybdenum roasted sand with a Mo mass fraction of 59.5% is added to the first ammonia leaching reactor 6 from the second feed pipe 4, and a first stirring rod 5 is used to stir to form a slurry, and the slurry temperature is controlled at 50-55° C., 70 ml of hydrogen peroxide is added to the second ammonia leaching reactor 11 from the third feed pipe 9, and 100 g of molybdenum roasted sand with a Mo mass fraction of 59.5% is added to the second ammonia leaching reactor 11 from the fourth feed pipe 10, and a second stirring rod 12 is used to stir to form a slurry, and the slurry temperature is controlled at 50-55° C. The first hydraulic jet pump 18 is turned on, and 105 ml of ammonia water with a mass fraction of 25% is dripped into the first ammonia leaching reactor 6 through the ammonia water storage tank 1, the first pipeline 21, the first high-level tank 2 and the second pipeline 22, and a second high-level tank 8 is added to the first ammonia leaching reactor 6 through the fourth pipeline 24, the second high-level tank 8 and the first high-level tank 9. The third pipeline 23 drips 105 ml of ammonia water with a mass fraction of 25% into the second ammonia leaching reactor 8. When the slurry temperature exceeds 55°C, the dripping is stopped, and when the temperature is lower than 50°C, the dripping is continued until the addition is completed. The second hydraulic jet pump 19 is turned on, and water is supplied to the two-stage spray tower 14 through the pure water inlet pipe 15 and the two-stage spray tower 14 is turned on. The third hydraulic jet pump 20 is turned on. The first ammonia leaching reactor 6 and the second ammonia leaching reactor 11 are connected in series in a closed negative pressure manner through the first tail gas pipe 7. The ammonia escaping from the first ammonia leaching reactor 6 under pressure enters the first ammonia leaching reactor 11 through the first tail gas pipe 7 to continue to dissolve the molybdenum roasted sand with ammonia, thereby minimizing the escape of ammonia. The unconsumed ammonia in the second ammonia leaching reactor 11 is absorbed by the two-stage spray tower 14, and then transported to the second high-level tank 8 through the ammonia solution transporting pipe 16 for recycling, thereby improving the utilization rate of ammonia and effectively controlling the unorganized emission of ammonia. Finally, 170 ml of ammonia leaching solution was obtained, Mo284.2 g / L, NH3 dosage was 112% of the theoretical value, and the primary leaching rate = 284.2 g / L*0.17 L / 100*59.5% = 81.2%.
[0026] Example 4
[0027] The device for reducing ammonia consumption in the process of ammonia leaching of molybdenum roasted sand proposed in this embodiment is as follows: Figure 1As shown, 85 ml of hydrogen peroxide is added to the first ammonia leaching reactor 6 from the first feed pipe 3, 100 g of molybdenum roasted sand with a Mo mass fraction of 58.2% is added to the first ammonia leaching reactor 6 from the second feed pipe 4, and a first stirring rod 5 is used to stir to form a slurry, and the slurry temperature is controlled at 50-55° C., 85 ml of hydrogen peroxide is added to the second ammonia leaching reactor 11 from the third feed pipe 9, and 100 g of molybdenum roasted sand with a Mo mass fraction of 58.2% is added to the second ammonia leaching reactor 11 from the fourth feed pipe 10, and a second stirring rod 12 is used to stir to form a slurry, and the slurry temperature is controlled at 50-55° C. The first hydraulic jet pump 18 is turned on, and 92 ml of ammonia water with a mass fraction of 28% is dripped into the first ammonia leaching reactor 6 through the ammonia water storage tank 1, the first pipeline 21, the first high-level tank 2 and the second pipeline 22, and a first stirring rod 5 is used to stir to form a slurry, and the slurry temperature is controlled at 50-55° C. The third pipeline 23 drips 92 ml of ammonia water with a mass fraction of 28% into the second ammonia leaching reactor 8. When the slurry temperature exceeds 55°C, the dripping is stopped, and when the temperature is lower than 50°C, the dripping is continued until the addition is completed. The second hydraulic jet pump 19 is turned on, and water is supplied to the two-stage spray tower 14 through the pure water inlet pipe 15 and the two-stage spray tower 14 is turned on. The third hydraulic jet pump 20 is turned on. The first ammonia leaching reactor 6 and the second ammonia leaching reactor 11 are connected in series in a closed negative pressure manner through the first tail gas pipe 7. The ammonia escaping from the first ammonia leaching reactor 6 under pressure enters the first ammonia leaching reactor 11 through the first tail gas pipe 7 to continue to dissolve the molybdenum roasted sand with ammonia, thereby minimizing the escape of ammonia. The unconsumed ammonia in the second ammonia leaching reactor 11 is absorbed by the two-stage spray tower 14, and then transported to the second high-level tank 8 through the ammonia solution transporting pipe 16 for recycling, thereby improving the utilization rate of ammonia and effectively controlling the unorganized emission of ammonia. Finally, 170 ml of ammonia leaching solution was obtained, Mo277.6 g / L, NH3 dosage was 112% of the theoretical value, and the first leaching rate = 277.6 g / L*0.17 L / 100*58.2% = 81.1%.
Claims
1. A device for reducing ammonia consumption in ammonia leaching process of molybdenum roasting, characterized in that: The invention comprises an ammonia water storage tank (1), wherein the ammonia water storage tank (1) is connected to a first high-level tank (2) via a first pipeline (21), the first high-level tank (2) is connected to a first ammonia leaching reactor (6) via a second pipeline (22), the first ammonia leaching reactor (6) is connected to a first feed pipe (3) and a second feed pipe (4), the first ammonia leaching reactor (6) is connected to a second high-level tank (8) via a first tail gas pipe (7), and the second high-level tank (8) is connected to the first pipeline via a third pipeline (23). (21), the second high-level tank (8) is connected to the second ammonia leaching reactor (11) through the fourth pipeline (24), the second ammonia leaching reactor (11) is connected to the third feed pipe (9) and the fourth feed pipe (10), the second ammonia leaching reactor (11) is connected to the two-stage spray tower (14) through the second tail gas pipe (13), the two-stage spray tower (14) is connected to the pure water inlet pipe (15), and the two-stage spray tower (14) is connected to the second high-level tank (8) through the ammonia solution outlet pipe (16).
2. The device for reducing ammonia consumption in ammonia leaching process of molybdenum roasting according to claim 1, characterized in that: A first stirring rod (5) is provided in the first ammonia leaching reaction kettle (6).
3. The device for reducing ammonia consumption in ammonia leaching process of molybdenum roasting according to claim 1, characterized in that: A second stirring rod (12) is provided in the second ammonia leaching reaction kettle (11).
4. The device for reducing ammonia consumption in ammonia leaching process of molybdenum roasting according to claim 1, characterized in that: The first pipeline (21) is provided with a valve (17).
5. The device for reducing ammonia consumption in ammonia leaching process of molybdenum roasting according to claim 1, characterized in that: The first tail gas pipe (7) is provided with a first hydraulic jet pump (18).
6. The device for reducing ammonia consumption in ammonia leaching process of molybdenum roasting according to claim 1, characterized in that: The second tail gas pipe (13) is provided with a second hydraulic jet pump (19).
7. The device for reducing ammonia consumption in ammonia leaching process of molybdenum roasting according to claim 1, characterized in that: A third hydraulic jet pump (20) is provided on the ammonia solution outlet pipe (16).