Washing, dedusting and purifying device and roasting flue gas treatment system

Abstract

The invention provides a washing, dedusting and purifying device and a roasting flue gas treatment system, and relates to the technical field of metallurgy. The washing, dedusting and purifying device comprises a first washing pipe, a first connecting pipe and a first gas-liquid separation tank; the first washing pipe is sleeved with a cooling jacket, and the first washing pipe is connected with the first connecting pipe; a first liquid inlet pipe is arranged on the first connecting pipe in a penetrating mode, a first nozzle is arranged on the first liquid inlet pipe and faces the first washing pipe, and the first connecting pipe is arranged in the tangential direction of the first gas-liquid separation tank and connected with the upper portion of the side wall of the first gas-liquid separation tank. The washing, dedusting and purifying device can replace conventional electric dust collection equipment to efficiently dedust and purify high-temperature and high-dust-content flue gas, the defect that the electric dust collection equipment in a conventional dry dust collection technology is prone to dew point corrosion is overcome under the condition that the dedusting efficiency is guaranteed, and the maintenance workload of equipment pipelines is greatly reduced; meanwhile, the adverse effect of the low-concentration sulfur dioxide flue gas on the subsequent acid making operation is improved.

Description

Technical Field

[0001] The present invention relates to the technical field of metallurgy, and in particular to a washing, dust removal and purification device and a roasting fume treatment system. Background Art

[0002] The common flue gas treatment system for copper (cobalt) sulfide ore roasting involves fluidized bed roasting, flue gas dust collection, acid purification, roasted sand acid leaching, leachate extraction and enrichment, and electrolytic deposition to produce cathode copper. During the fluidized bed roasting process, the flue gas contains a large amount of fine particulate matter (smoke dust), sulfur dioxide (SO2), and sulfur trioxide (SO3). Conventional processes use cyclonic dust collection followed by high-temperature electrostatic precipitators to efficiently recover fine particulate matter from the flue gas.

[0003] However, due to the high sulfur trioxide concentration and dew point temperature in the flue gas of sulfated / semi-sulfated roasting, the electrostatic precipitator often suffers from dew point corrosion during long-term operation. This not only causes a large workload for maintenance of the electrostatic precipitator pipeline, but also leads to a rapid increase in system air leakage, diluting the sulfur dioxide concentration in the flue gas, and adversely affecting subsequent flue gas acid production operations. Summary of the Invention

[0004] In order to solve the problems existing in the prior art, one of the purposes of the present invention is to provide a washing, dust removal and purification device.

[0005] The present invention provides the following technical solutions:

[0006] A washing and dust removal purification device comprises a first washing pipe, a first connecting pipe and a first gas-liquid separation tank;

[0007] The first washing pipe is provided with a cooling jacket, one end of the first washing pipe is provided with a smoke inlet, and the other end is connected to the first connecting pipe;

[0008] A first liquid inlet pipe is passed through the first connecting pipe, and a first nozzle is provided at one end of the first liquid inlet pipe located inside the first connecting pipe, and the first nozzle is arranged toward the first washing pipe. An end of the first connecting pipe away from the first washing pipe is arranged tangentially along the first gas-liquid separation tank and connected to the upper portion of the side wall of the first gas-liquid separation tank;

[0009] A gas outlet pipe is provided on the top of the first gas-liquid separation tank, and a liquid discharge port is provided on the bottom.

[0010] As a further optional solution for the washing, dust removal and purification device, the inner wall of the first washing pipe is provided with a first spiral guide vane.

[0011] As a further optional solution for the washing and dust removal purification device, the width of the first spiral guide vane along the radial direction of the first washing pipe is W1, 20mm≤W1≤50mm; and / or

[0012] The pitch of the first spiral guide vane is H1, the diameter of the first washing pipe is D1, and 0.5≤H1 / D1≤1.5.

[0013] As a further optional solution for the washing and dust removal purification device, the inner wall of the first gas-liquid separation tank is provided with a second spiral guide vane.

[0014] As a further optional solution for the scrubbing and dust removal purification device, the width of the second spiral guide vane along the radial direction of the first gas-liquid separation tank is W2, 20mm≤W2≤50mm; and / or

[0015] The pitch of the second spiral guide vane is H2, the diameter of the first gas-liquid separation tank is D2, and 0.1≤H2 / D2≤1.2.

[0016] As a further optional solution to the washing and dust removal purification device, the washing and dust removal purification device further includes a raffinate pipe and a first circulation pump;

[0017] One end of the raffinate pipe is connected to the first gas-liquid separation tank, and the other end is used to connect to the extraction device of the hydrometallurgical system, and the drain port is used to connect to the leaching device of the hydrometallurgical system;

[0018] The inlet of the first circulation pump is connected to the lower part of the first gas-liquid separation tank, and the outlet of the first circulation pump is connected to the first liquid inlet pipe.

[0019] Another object of the present invention is to provide a roasting flue gas treatment system.

[0020] The present invention provides the following technical solutions:

[0021] A roasting flue gas treatment system comprises a cooling and scrubbing tower, an electrostatic precipitator and the above-mentioned scrubbing and dust removal purification device, wherein the gas inlet of the cooling and scrubbing tower is connected to the gas outlet pipe, and the inlet of the electrostatic precipitator is connected to the gas outlet of the cooling and scrubbing tower.

[0022] As a further optional solution to the roasting flue gas treatment system, the roasting flue gas treatment system further includes a second circulation pump, a primary circulating water cooling heat exchanger and a secondary cryogenic heat exchanger;

[0023] The inlet of the second circulation pump is connected to the liquid outlet of the cooling and washing tower, the outlet of the second circulation pump is connected to the inlet of the primary circulating water cooling heat exchanger, the outlet of the primary circulating water cooling heat exchanger is connected to the inlet of the secondary cryogenic heat exchanger, and the outlet of the secondary cryogenic heat exchanger is connected to the liquid inlet of the cooling and washing tower.

[0024] As a further optional solution to the roasting fume treatment system, the roasting fume treatment system further includes a low-temperature washing device, which is arranged between the washing and dust removal purification device and the cooling and washing tower, and includes a second washing pipe, a second connecting pipe, a second gas-liquid separation tank and a third circulation pump;

[0025] One end of the second washing pipe is connected to the gas outlet pipe, and the other end is connected to the second connecting pipe. A second liquid inlet pipe is passed through the second connecting pipe. A second nozzle is provided at one end of the second liquid inlet pipe located in the second connecting pipe, and the second nozzle is arranged toward the second washing pipe. An end of the second connecting pipe away from the second washing pipe is connected to the upper part of the side wall of the second gas-liquid separation tank, the gas outlet of the second gas-liquid separation tank is connected to the gas inlet of the cooling washing tower, the inlet of the third circulating pump is connected to the liquid outlet of the second gas-liquid separation tank, and the outlet of the third circulating pump is connected to the second liquid inlet pipe.

[0026] As a further optional solution to the roasting fume treatment system, the cooling and washing tower is connected to a clean water pipe;

[0027] The second gas-liquid separation tank is connected to a third liquid inlet pipe, and the third liquid inlet pipe is connected to the liquid outlet of the cooling and washing tower;

[0028] The first gas-liquid separation tank is connected to a fourth liquid inlet pipe, and the fourth liquid inlet pipe is connected to the outlet of the third circulation pump.

[0029] The embodiments of the present invention have the following beneficial effects:

[0030] When using the above-described scrubbing and dust removal purification device, the high-temperature, dust-laden flue gas to be treated enters the first scrubbing pipe through the flue gas inlet. Simultaneously, scrubbing liquid is delivered to the first nozzle via the first liquid inlet pipe and ejected toward the first scrubbing pipe, impacting the high-temperature, dust-laden flue gas in a countercurrent direction. This scrubbing action causes fine particulate matter in the high-temperature, dust-laden flue gas to mix with the scrubbing liquid, and also dissolves sulfur dioxide and sulfur trioxide in the high-temperature, dust-laden flue gas. During this process, the coolant absorbs heat as it flows within the cooling jacket, rapidly cooling the high-temperature, dust-laden flue gas and achieving adiabatic evaporation. Subsequently, the gas-liquid mixed fluid enters the upper sidewall of the first gas-liquid separator tank through the first connecting pipe, spiraling downward along the inner wall of the first gas-liquid separator tank. Centrifugal force separates the gas phase from the liquid and solid phases. Finally, the dust-laden scrubbing liquid is discharged through the drain port at the bottom of the first gas-liquid separator tank, and the purified gas phase is discharged through the gas outlet pipe at the top of the first gas-liquid separator tank. Therefore, the above-mentioned washing dust removal and purification device can replace conventional electrostatic precipitators to perform efficient dust removal and purification on high-temperature and high-dust flue gas. While ensuring the dust removal efficiency, it avoids the disadvantage that the electrostatic precipitator equipment in conventional dry dust collection technology is prone to dew point corrosion, greatly reduces the workload of equipment pipeline maintenance, and at the same time improves the adverse effects of low-concentration sulfur dioxide flue gas on subsequent acid production operations.

[0031] In order to make the above-mentioned objects, features and advantages of the present invention more obvious and easy to understand, preferred embodiments are given below and described in detail with reference to the accompanying drawings. BRIEF DESCRIPTION OF THE DRAWINGS

[0032] In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the following briefly introduces the drawings required for use in the embodiments. It should be understood that the following drawings only illustrate certain embodiments of the present invention and therefore should not be regarded as limiting the scope. For ordinary technicians in this field, other relevant drawings can be obtained based on these drawings without paying any creative work.

[0033] Figure 1 The figure shows the overall structure of a washing and dust removal purification device provided by an embodiment of the present invention;

[0034] Figure 2 The figure shows the overall structure of a roasting flue gas treatment system provided by an embodiment of the present invention;

[0035] Figure 3 A schematic structural diagram of a scrubbing and dust removal purification device in a roasting flue gas treatment system provided by an embodiment of the present invention is shown;

[0036] Figure 4 A schematic structural diagram of a low-temperature scrubbing device in a roasting flue gas treatment system provided by an embodiment of the present invention is shown.

[0037] Description of main component symbols:

[0038] 100 - washing and dust removal device; 110 - first washing pipe; 111 - cooling jacket; 112 - flue gas inlet; 113 - first spiral guide vane; 120 - first connecting pipe; 121 - first liquid inlet pipe; 122 - first nozzle; 130 - first gas-liquid separation tank; 131 - gas outlet pipe; 132 - liquid outlet; 133 - second spiral guide vane; 134 - fourth liquid inlet pipe; 140 - raffinate pipe; 150 - first circulation pump; 200 - cooling and washing tower; 2 10-clean water pipe; 300-electric demister; 400-low-temperature washing device; 410-second washing pipe; 420-second connecting pipe; 421-second liquid inlet pipe; 422-second nozzle; 430-second gas-liquid separation tank; 431-third liquid inlet pipe; 440-third circulating pump; 500-second circulating pump; 600-first-stage circulating water cooling heat exchanger; 700-second-stage deep-cold heat exchanger; 710-heat exchanger; 720-chiller; 800-fourth circulating pump. DETAILED DESCRIPTION

[0039] The following describes embodiments of the present invention in detail. Examples of the embodiments are shown in the accompanying drawings, wherein the same or similar reference numerals throughout represent the same or similar elements or elements having the same or similar functions. The embodiments described below with reference to the accompanying drawings are exemplary and are intended only to explain the present invention and are not to be construed as limiting the present invention.

[0040] It should be noted that when an element is referred to as being "fixed to" another element, it may be directly on the other element or there may be an intermediate element. When an element is considered to be "connected to" another element, it may be directly connected to the other element or there may be an intermediate element. Conversely, when an element is referred to as being "directly on" another element, there is no intermediate element. The terms "vertical," "horizontal," "left," "right," and similar expressions used herein are for illustrative purposes only.

[0041] In the present invention, unless otherwise expressly specified or limited, the terms "mounted," "connected," "connect," "fixed," etc. should be understood broadly. For example, they may refer to fixed connection, detachable connection, or integration; mechanical connection or electrical connection; direct connection or indirect connection through an intermediate medium; internal communication between two components or interaction between two components. Those skilled in the art will understand the specific meanings of the above terms in the present invention based on specific circumstances.

[0042] Furthermore, the terms "first" and "second" are used for descriptive purposes only and should not be construed as indicating or implying relative importance or implicitly specifying the number of the technical features being referred to. Thus, a feature identified as "first" or "second" may explicitly or implicitly include one or more of the features. In the description of the present invention, "plurality" means two or more, unless otherwise specifically defined.

[0043] Unless otherwise defined, all technical and scientific terms used herein have the same meaning as commonly understood by those skilled in the art to which this application belongs. The terms used in the template description herein are for the purpose of describing specific embodiments only and are not intended to limit the present invention. The term "and / or" as used herein includes any and all combinations of one or more of the associated listed items.

[0044] The inventors of the present application have discovered that conventional boiling (sulfation / semi-acidification / oxidation) roasting flue gas is generally followed by cyclone dust collection to set up high-temperature electrostatic precipitators to efficiently recover fine particulate matter in the flue gas. However, due to the high concentration of sulfur trioxide and the high dew point temperature in the sulfated / semi-sulfated roasting flue gas, the electrostatic precipitator basically has dew point corrosion problems during long-term operation. Even if measures such as heat preservation and heating, and improving the corrosion resistance of wall panels are adopted, it is still impossible to completely avoid the problem of corrosion and leakage at local low temperatures inside. Once a leak occurs, the low temperature point will accelerate the corrosion of the electrostatic precipitator pipeline, forming more leaks. Not only does it cause a large workload for the maintenance of the electrostatic precipitator pipeline, it also leads to a rapid increase in the system leakage, diluting the sulfur dioxide concentration in the flue gas, and adversely affecting the subsequent flue gas acid production operation.

[0045] Furthermore, the SO concentration in the flue gas from copper (cobalt) sulfide ore roasting is relatively low (typically 3%-4%), making a one-turn, one-absorption acidification process theoretically feasible. Conventional purification and scrubbing processes utilize packed tower scrubbing, with circulating water and scrubbing fluid indirectly exchanging heat during the process. However, due to the high circulating water temperature (32-42°C), the flue gas temperature at the purification section outlet can typically only be reduced to 36°C, resulting in excessively high saturated water content in the flue gas, making it difficult to maintain water balance during the one-turn, one-absorption acidification process.

[0046] Example 1

[0047] In response to the above problems, this embodiment provides a washing and dust removal purification device 100, specifically a fast iterative washing and dust removal purification device for treating high-temperature and high-dust flue gas.

[0048] For example, the high-temperature and high-dust flue gas comes from a smelting process, with a temperature of 150-400°C and a dust concentration of 1-50g / Nm 3 .

[0049] See also Figure 1The washing and dust removal purification device 100 includes a first washing pipe 110 , a first connecting pipe 120 and a first gas-liquid separation tank 130 .

[0050] The first washing pipe 110 is provided with a cooling jacket 111 . A fume inlet 112 is provided at one end of the first washing pipe 110 , and the other end is connected to the first connecting pipe 120 .

[0051] A first liquid inlet pipe 121 is provided through the first connecting pipe 120. A first nozzle 122 is provided at one end of the first liquid inlet pipe 121 located within the first connecting pipe 120, and the first nozzle 122 is positioned toward the first washing pipe 110. The end of the first connecting pipe 120, away from the first washing pipe 110, is disposed tangentially to the first gas-liquid separator tank 130 and is connected to the upper portion of the side wall of the first gas-liquid separator tank 130.

[0052] In addition, a gas outlet pipe 131 is provided on the top of the first gas-liquid separation tank 130 , and a liquid drain port 132 is provided on the bottom.

[0053] When the above-mentioned washing and dust removal purification device 100 is used, the high-temperature and high-dust flue gas to be treated enters the first washing pipe 110 through the flue gas inlet 112. At the same time, the washing liquid is transported to the first nozzle 122 through the first liquid inlet pipe 121 and sprayed toward the first washing pipe 110, impacting the high-temperature and high-dust flue gas in the opposite direction, washing the high-temperature and high-dust flue gas, so that the fine particulate matter in the high-temperature and high-dust flue gas is mixed with the washing liquid, and the sulfur dioxide and sulfur trioxide in the high-temperature and high-dust flue gas are dissolved in the washing liquid. In this process, the coolant flows in the cooling jacket 111 and absorbs heat, causing the high-temperature and high-dust flue gas to quickly cool down and complete adiabatic evaporation. Subsequently, the gas-liquid mixed fluid enters the upper part of the side wall of the first gas-liquid separation tank 130 along the tangent direction of the first gas-liquid separation tank 130 through the first connecting pipe 120, spirals downward along the inner wall of the first gas-liquid separation tank 130, and completes the separation of the gas phase from the liquid phase and the solid phase under the action of centrifugal force. Finally, the dust-laden washing liquid is discharged from the drain port 132 at the bottom of the first gas-liquid separation tank 130 , and the purified gas phase is discharged from the gas outlet pipe 131 at the top of the first gas-liquid separation tank 130 .

[0054] Therefore, the above-mentioned washing dust removal and purification device 100 can replace conventional electrostatic precipitators to perform efficient dust removal and purification on high-temperature and high-dust flue gas. While ensuring the dust removal efficiency, it avoids the disadvantage that the electrostatic precipitator equipment in conventional dry dust collection technology is prone to dew point corrosion, greatly reduces the workload of equipment pipeline maintenance, and at the same time improves the adverse effects of low-concentration sulfur dioxide flue gas on subsequent acid production operations.

[0055] In some embodiments, first scrubber 110 is a high-temperature resistant, cylindrical, and vertically arranged scrubber. A flue gas inlet 112 is located at the top of first scrubber 110 and is provided with a connecting flange for connecting to an external air intake pipe. A first connecting pipe 120 is connected to the bottom of first scrubber 110. Accordingly, a first nozzle 122 is located directly below first scrubber 110. After entering first nozzle 122, scrubber liquid is sprayed upward.

[0056] Furthermore, a first spiral guide vane 113 is provided on the inner wall of the first washing pipe 110 .

[0057] When the high-temperature and high-dust flue gas to be treated enters the first washing pipe 110 through the flue gas inlet 112, the first spiral guide vane 113 can disturb the high-temperature and high-dust flue gas, increase its turbulence, increase the gas-liquid mass transfer and heat transfer effect, achieve rapid cooling of the flue gas, and enhance the three-phase mixing effect.

[0058] For example, the first washing pipe 110 and the first spiral guide vane 113 are made of Hastelloy, Monel or equivalent alloy materials, and the cooling jacket 111 is made of carbon steel. In addition, the coolant flowing into the cooling jacket 111 is circulating water.

[0059] Optionally, the width of the first spiral guide vane 113 along the radial direction of the first washing pipe 110 is W1, which satisfies 20 mm ≤ W1 ≤ 50 mm.

[0060] Setting the width of the first spiral guide vanes 113 along the radial direction of the first washing pipe 110 to be no less than 20 mm ensures that the first spiral guide vanes 113 have a sufficient disturbing effect on the high-temperature, high-dust flue gas. Conversely, setting the width of the first spiral guide vanes 113 along the radial direction of the first washing pipe 110 to be no greater than 50 mm prevents the high-temperature, high-dust flue gas from encountering excessive resistance when it contacts the first spiral guide vanes 113, thereby facilitating the smooth flow of the high-temperature, high-dust flue gas.

[0061] For example, the width of the first spiral guide vane 113 along the radial direction of the first washing pipe 110 may be 20 mm, 25 mm, 30 mm, 35 mm, 40 mm, 45 mm, 50 mm, or any value between 20 mm and 50 mm.

[0062] Optionally, the pitch of the first spiral guide vane 113 is H1, and the diameter of the first washing pipe 110 is D1, satisfying 0.5≤H1 / D1≤1.5.

[0063] Setting the ratio of the pitch of the first spiral guide vane 113 to the diameter of the first washing pipe 110 to no greater than 1.5 ensures that the first spiral guide vane 113 has a sufficient disturbing effect on the high-temperature, high-dust flue gas. Conversely, setting the ratio of the pitch of the first spiral guide vane 113 to the diameter of the first washing pipe 110 to no less than 0.5 prevents the high-temperature, high-dust flue gas from encountering excessive resistance when it contacts the first spiral guide vane 113, thereby facilitating the smooth flow of the high-temperature, high-dust flue gas.

[0064] Illustratively, the ratio of the pitch of the first helical guide vane 113 to the diameter of the first washing pipe 110 may be 0.5, 0.6, 0.7, 0.8, 0.9, 1, 1.1, 1.2, 1.3, 1.4, 1.5, or any value between 0.5 and 1.5.

[0065] In some embodiments, the first connecting pipe 120 is composed of a connecting elbow and an expansion joint. The connecting elbow is vertically arranged at one end near the first washing pipe 110 and connected to the first washing pipe 110 through the expansion joint. The connecting elbow is horizontally arranged at one end near the first gas-liquid separation tank 130.

[0066] In some embodiments, the first gas-liquid separation tank 130 comprises a cylindrical tank body and a conical bottom. The tank body is vertically arranged, with the conical bottom connected to the bottom end of the tank body. Accordingly, the first connecting pipe 120 is connected to the upper sidewall of the tank body, and the gas outlet pipe 131 is provided through the top of the tank body. Furthermore, a liquid drain port 132 is provided at the bottom end of the conical bottom.

[0067] Furthermore, a second spiral guide vane 133 is provided on the inner wall of the first gas-liquid separation tank 130 .

[0068] When the gas-liquid mixed fluid enters the first gas-liquid separation tank 130 , the second spiral guide vane 133 can guide the gas-liquid mixed fluid to spiral downward better, thereby achieving enhanced efficient separation of the gas phase from the liquid phase and the solid phase under the action of centrifugal force.

[0069] Optionally, the width of the second spiral guide vane 133 along the radial direction of the first gas-liquid separation tank 130 is W2, which satisfies 20 mm ≤ W2 ≤ 50 mm.

[0070] Setting the width of the second spiral guide vanes 133 along the radial direction of the first gas-liquid separation tank 130 to be no less than 20 mm ensures that the second spiral guide vanes 133 provide sufficient guidance for the gas-liquid mixed fluid. Conversely, setting the width of the second spiral guide vanes 133 along the radial direction of the first gas-liquid separation tank 130 to be no greater than 50 mm prevents the gas-liquid mixed fluid from experiencing excessive resistance when contacting the second spiral guide vanes 133, thereby facilitating smooth flow of the gas-liquid mixed fluid.

[0071] Exemplarily, the width of the second spiral guide vane 133 along the radial direction of the first gas-liquid separation tank 130 can be 20 mm, 25 mm, 30 mm, 35 mm, 40 mm, 45 mm, 50 mm, or any value between 20 mm and 50 mm.

[0072] Optionally, the pitch of the second spiral guide vane 133 is H2, and the diameter of the first gas-liquid separation tank 130 is D2, satisfying 0.1≤H2 / D2≤1.2.

[0073] Setting the ratio of the pitch of the second spiral guide vane 133 to the diameter of the first gas-liquid separation tank 130 to no greater than 1.2 ensures that the second spiral guide vane 133 provides sufficient guidance for the gas-liquid mixed fluid. Conversely, setting the ratio of the pitch of the second spiral guide vane 133 to the diameter of the first gas-liquid separation tank 130 to no less than 0.1 prevents the gas-liquid mixed fluid from experiencing excessive resistance when contacting the second spiral guide vane 133, thereby facilitating smooth flow of the gas-liquid mixed fluid.

[0074] Illustratively, the ratio of the pitch of the second helical guide vane 133 to the diameter of the first gas-liquid separation tank 130 may be 0.1, 0.2, 0.3, 0.4, 0.5, 0.6, 0.7, 0.8, 0.9, 1, 1.1, 1.2, or any value between 0.1 and 1.2.

[0075] Optionally, the lower edge of the gas outlet pipe 131 is lower than the bottom of the first connecting pipe 120 , and the height difference between the lower edge of the gas outlet pipe 131 and the bottom of the first connecting pipe 120 is 200-500 mm.

[0076] Optionally, the angle of the cone bottom of the first gas-liquid separation tank 130 is 60-90°.

[0077] Please also refer to Figure 2 and Figure 3 In some embodiments, the washing and dust removal purification device 100 further includes a raffinate pipe 140 and a first circulation pump 150 .

[0078] One end of the raffinate pipe 140 is connected to the first gas-liquid separation tank 130, and the other end is used to connect to the extraction device of the hydrometallurgical system. Correspondingly, the drain port 132 is used to connect to the leaching device of the hydrometallurgical system.

[0079] In addition, an inlet of the first circulation pump 150 is connected to the lower portion of the first gas-liquid separation tank 130 , and an outlet of the first circulation pump 150 is connected to the first liquid inlet pipe 121 .

[0080] It can be understood that the raffinate in the extraction-electrodeposition process is relatively clean. The raffinate is introduced from the extraction device of the hydrometallurgical system into the first gas-liquid separation tank 130 through the raffinate pipe 140, and the raffinate accumulated in the lower part of the first gas-liquid separation tank 130 is pumped to the first liquid inlet pipe 121 by the first circulation pump 150, so that the raffinate is used as a washing liquid to wash the high-temperature and high-dust flue gas, which can effectively reduce the consumption of new water. While reducing water consumption, it also alleviates the water circulation imbalance problem in the roasted sand leaching process and the extraction process of the hydrometallurgical system.

[0081] It should be noted that as the scrubbing process continues, more and more fine particulate matter is mixed into the raffinate, causing it to become increasingly turbid. Because the inlet of the first circulating pump 150 is connected to the lower portion of the first gas-liquid separator tank 130 rather than its bottom end, the raffinate pumped by the first circulating pump 150 to the first liquid inlet pipe 121 is a supernatant with a relatively low concentration of particulate matter, thereby ensuring a scrubbing effect on the high-temperature, dust-laden flue gas.

[0082] Correspondingly, the lower layer of dust-containing washing liquid with a relatively high concentration of particulate matter is discharged to the leaching device of the hydrometallurgical system through the drain port 132, so that the raffinate can be returned to the roasted sand leaching process for continued recycling.

[0083] During this process, new raffinate is continuously added to the first gas-liquid separation tank 130 , and the particulate matter concentration of the raffinate used to wash the high-temperature and high-dust flue gas is controlled below 10 g / L.

[0084] When using the above-mentioned scrubbing and dust removal purification device 100, the high-temperature, high-dust flue gas to be treated enters the first scrubbing pipe 110 through the flue gas inlet 112, and its turbulence is increased under the disturbance of the first spiral guide vane 113. At the same time, the raffinate is transported to the first nozzle 122 as a scrubbing liquid through the first liquid inlet pipe 121 and sprayed toward the first scrubbing pipe 110, impacting the high-temperature, high-dust flue gas in the opposite direction, scrubbing the high-temperature, high-dust flue gas, causing fine particulate matter in the high-temperature, high-dust flue gas to mix with the scrubbing liquid, and causing sulfur dioxide and sulfur trioxide in the high-temperature, high-dust flue gas to dissolve in the scrubbing liquid. During this process, the coolant flows in the cooling jacket 111 and absorbs heat, ensuring that the inner wall temperature of the first scrubbing pipe 110 is below 100°C, rapidly cooling the high-temperature, high-dust flue gas and completing adiabatic evaporation. The gas-liquid mixture then enters the upper sidewall of the first gas-liquid separator tank 130 through the first connecting pipe 120, along a tangential direction. Guided by the second spiral guide vanes 133, it spirals downward along the inner wall of the first gas-liquid separator tank 130, where centrifugal force separates the gas phase from the liquid and solid phases. Finally, the dust-laden scrubbing liquid is discharged through the drain port 132 at the bottom of the first gas-liquid separator tank 130, and the purified gas phase is discharged through the gas outlet pipe 131 at the top of the first gas-liquid separator tank 130.

[0085] Therefore, the above-mentioned washing dust removal and purification device 100 can replace conventional electrostatic precipitators to perform efficient dust removal and purification on high-temperature and high-dust flue gas. While ensuring the dust removal efficiency, it avoids the disadvantage that the electrostatic precipitator equipment in conventional dry dust collection technology is prone to dew point corrosion, greatly reduces the workload of equipment pipeline maintenance, and can also effectively save one-time investment costs, while improving the adverse effects of low-concentration sulfur dioxide flue gas on subsequent acid production operations.

[0086] In addition, the washing and dust removal purification device 100 effectively reduces the consumption of new water by introducing the circulation of the raffinate, and is also beneficial to alleviating the water circulation imbalance problem in the roasted sand leaching process and the extraction process of the hydrometallurgical system.

[0087] In summary, the above-mentioned washing dust removal and purification device 100 has the advantages of high dust removal efficiency, low equipment maintenance cost, good system stability, and resource recycling.

[0088] Example 2

[0089] This embodiment provides a roasting flue gas treatment system, specifically a high-efficiency wet dust removal and deep cooling purification system for flue gas from boiling roasting of copper (cobalt) sulfide concentrate.

[0090] See also Figure 2 The roasting flue gas treatment system includes a cooling and washing tower 200, an electrostatic precipitator 300 and the above-mentioned washing and dust removal purification device 100.

[0091] The gas inlet of the cooling and washing tower 200 is connected to the gas outlet pipe 131 , and the inlet of the electric precipitator 300 is connected to the gas outlet of the cooling and washing tower 200 .

[0092] During use, the gas phase purified by the washing and dust removal purification device 100 is discharged from the gas outlet pipe 131, enters the cooling and washing tower 200 to be washed and cooled again, and then passes through the electrostatic precipitator 300 to remove acid mist and fine particles. Finally, the purified flue gas is sent to the acid production system.

[0093] Please also refer to Figure 2 and Figure 4 In some embodiments, the roasting flue gas treatment system further includes a low-temperature scrubbing device 400. The low-temperature scrubbing device 400 is disposed between the scrubbing and dust removal purification device 100 and the cooling scrubbing tower 200. The low-temperature scrubbing device 400 includes a second scrubbing pipe 410, a second connecting pipe 420, a second gas-liquid separation tank 430, and a third circulating pump 440.

[0094] One end of the second washing pipe 410 is connected to the gas outlet pipe 131, and the other end is connected to the second connecting pipe 420. A second liquid inlet pipe 421 is provided on the second connecting pipe 420. A second nozzle 422 is provided at one end of the second liquid inlet pipe 421 located within the second connecting pipe 420, and the second nozzle 422 is positioned toward the second washing pipe 410. The end of the second connecting pipe 420, away from the second washing pipe 410, is connected to the upper sidewall of the second gas-liquid separator tank 430. The gas outlet of the second gas-liquid separator tank 430 is connected to the gas inlet of the cooling scrubber 200. The inlet of the third circulating pump 440 is connected to the liquid outlet of the second gas-liquid separator tank 430, and the outlet of the third circulating pump 440 is connected to the second liquid inlet pipe 421.

[0095] During use, the gas phase purified by the washing and dust removal purification device 100 is discharged from the gas outlet pipe 131 and directly enters the second washing pipe 410. At the same time, the third circulation pump 440 pumps the washing liquid accumulated at the bottom of the second gas-liquid separator 430 to the second liquid inlet pipe 421, and then the washing liquid is sprayed toward the second washing pipe 410 through the second nozzle 422, impacting the flue gas in the opposite direction, washing the flue gas again, further reducing the flue gas temperature and removing residual smoke. Subsequently, the gas-liquid mixed fluid enters the second gas-liquid separator 430 along the tangent direction of the second gas-liquid separator 430 through the second connecting pipe 420, spirals downward along the inner wall of the second gas-liquid separator 430, and completes the separation of the gas phase and the liquid phase under the action of centrifugal force. The liquid phase (i.e., the washing liquid) accumulates at the bottom of the second gas-liquid separator 430 and continues to be recycled. The gas phase after being purified again is discharged to the cooling washing tower 200 through the gas outlet at the top of the second gas-liquid separator 430.

[0096] Therefore, the flue gas undergoes two-stage washing before entering the cooling washing tower 200, and the washing effect is better.

[0097] For example, the washing liquid used in the low-temperature washing device 400 may be clean water or a low-concentration raffinate.

[0098] See also Figure 2 In some embodiments, the roasting flue gas treatment system further includes a second circulation pump 500 , a primary circulating water cooling heat exchanger 600 and a secondary cryogenic heat exchanger 700 .

[0099] The inlet of the second circulating pump 500 is connected to the liquid outlet of the cooling and washing tower 200, and the outlet of the second circulating pump 500 is connected to the inlet of the primary circulating water cooling heat exchanger 600. The outlet of the primary circulating water cooling heat exchanger 600 is connected to the inlet of the secondary cryogenic heat exchanger 700. The outlet of the secondary cryogenic heat exchanger 700 is connected to the liquid inlet of the cooling and washing tower 200.

[0100] Specifically, the primary circulating water cooling heat exchanger 600 adopts a conventional heat exchange structure and uses circulating water as the coolant.

[0101] The secondary cryogenic heat exchanger 700 is composed of a heat exchanger 710 and a chiller 720. The chiller 720 uses circulating water as a coolant and outputs chilled water at a lower temperature to the heat exchanger 710, where it exchanges heat with the washing liquid.

[0102] During operation, the second circulating pump 500 pumps the scrubbing liquid collected at the bottom of the cooling and scrubbing tower 200 to the primary circulating water cooling heat exchanger 600. The scrubbing liquid exchanges heat with the circulating cooling water in the primary circulating water cooling heat exchanger 600, cooling it to 34-36°C. The scrubbing liquid then enters the secondary cryogenic heat exchanger 700, exchanging heat with the chilled water provided by the chiller 720, cooling it to 24-28°C. Finally, the scrubbing liquid enters the liquid inlet at the top of the cooling and scrubbing tower 200, spraying and scrubbing the flue gas within the cooling and scrubbing tower 200.

[0103] During the washing process, the secondary deep cooling of the washing liquid can reduce the flue gas temperature to 26-30°C, thereby reducing the saturated water content in the flue gas and meeting the water balance requirements of the subsequent one-to-one absorption acid production.

[0104] Please also refer to Figure 2 、 Figure 3 and Figure 4 Furthermore, a clean water pipe 210 is connected to the cooling and washing tower 200 .

[0105] Correspondingly, the second gas-liquid separation tank 430 is connected to a third liquid inlet pipe 431 , and the third liquid inlet pipe 431 is connected to the liquid outlet of the cooling and washing tower 200 , specifically, to the outlet of the second circulation pump 500 .

[0106] In addition, a fourth liquid inlet pipe 134 is connected to the first gas-liquid separation tank 130 , and the fourth liquid inlet pipe 134 is connected to the outlet of the third circulation pump 440 .

[0107] During use, clean water can be added to the cooling and washing tower 200 through the clean water pipe 210, thereby reducing the ion concentration of the washing liquid in the cooling and washing tower 200. At the same time, the second circulating pump 500 pumps part of the washing liquid in the cooling and washing tower 200 to the second gas-liquid separator tank 430 through the third liquid inlet pipe 431, thereby reducing the ion concentration of the washing liquid in the second gas-liquid separator tank 430. The third circulating pump 440 pumps part of the washing liquid in the second gas-liquid separator tank 430 to the first gas-liquid separator tank 130 through the fourth liquid inlet pipe 134, thereby reducing the ion concentration of the washing liquid in the first gas-liquid separator tank 130.

[0108] Therefore, by adding clean water, the ion concentration of the washing liquid in various places in the entire roasting flue gas treatment system can be reduced, thereby reducing the ion concentration in the droplets discharged with the flue gas, avoiding affecting the subsequent acid production process.

[0109] In some embodiments, the roasting flue gas treatment system further includes a fourth circulation pump 800. The inlet of the fourth circulation pump 800 is connected to the drain port 132 of the first gas-liquid separation tank 130, and the outlet of the fourth circulation pump 800 is connected to the leaching device of the hydrometallurgical system.

[0110] During use, the fourth circulating pump 800 is used to discharge the dust-containing washing liquid in the lower layer, so that the raffinate is returned to the roasted sand leaching process for continued recycling.

[0111] In some embodiments, two electric demisters 300 are provided, and the two electric demisters 300 are connected in series.

[0112] After passing through the two-stage electrostatic precipitator 300, the concentration of particulate matter in the flue gas can be reduced to 2mg / Nm 3 , the acid mist concentration can be reduced to 5mg / Nm 3 .

[0113] In summary, the roasting flue gas treatment system uses a scrubbing dust removal and purification device 100 instead of an electrostatic precipitator, avoiding air leakage caused by dew point corrosion, and further avoiding the dilution of SO2 concentration in the flue gas due to air leakage, thereby ensuring the stability of subsequent flue gas acid production operations. Its scrubbing dust removal and purification device 100 has a simple structure and strong corrosion resistance, significantly reducing the maintenance workload of the equipment pipeline. At the same time, the roasting flue gas treatment system uses raffinate as a washing liquid, realizing resource recycling, reducing the consumption of new water, and alleviating the problem of water cycle imbalance in the roasted sand leaching-extraction process of the wet smelting system. In addition, the roasting flue gas treatment system reduces the flue gas temperature to 26-30°C through secondary deep cooling, solving the water balance problem in the one-turn-one-absorption acid production process.

[0114] In all examples shown and described herein, any specific values should be interpreted as merely exemplary and not limiting, and thus other examples of the exemplary embodiments may have different values.

[0115] It should be noted that similar reference numerals and letters denote similar items in the following drawings, and therefore, once an item is defined in one drawing, it does not need to be further defined or explained in subsequent drawings.

[0116] The above-described embodiments merely illustrate several implementations of the present invention, and while the descriptions are relatively specific and detailed, they should not be construed as limiting the scope of the present invention. It should be noted that variations and modifications are possible without departing from the scope of the present invention, and such variations and modifications are fully within the scope of protection of the present invention.

Claims

1. A washing and dust removal purification device, characterized in that: It includes a first washing pipe, a first connecting pipe and a first gas-liquid separation tank; The first washing pipe is provided with a cooling jacket, one end of the first washing pipe is provided with a smoke inlet, and the other end is connected to the first connecting pipe; A first liquid inlet pipe is passed through the first connecting pipe, and a first nozzle is provided at one end of the first liquid inlet pipe located inside the first connecting pipe, and the first nozzle is arranged toward the first washing pipe. An end of the first connecting pipe away from the first washing pipe is arranged tangentially along the first gas-liquid separation tank and connected to the upper portion of the side wall of the first gas-liquid separation tank; A gas outlet pipe is provided on the top of the first gas-liquid separation tank, and a liquid discharge port is provided on the bottom.

2. The washing and dust removal purification device according to claim 1, characterized in that: The inner wall of the first washing pipe is provided with a first spiral guide vane.

3. The washing and dust removal purification device according to claim 2, characterized in that: The width of the first spiral guide vane along the radial direction of the first washing pipe is W1, 20mm≤W1≤50mm; and / or The pitch of the first spiral guide vane is H1, the diameter of the first washing pipe is D1, and 0.5≤H1 / D1≤1.

5.

4. The washing and dust removal purification device according to claim 1, characterized in that: The inner wall of the first gas-liquid separation tank is provided with a second spiral guide vane.

5. The washing and dust removal device according to claim 4, characterized in that: The width of the second spiral guide vane along the radial direction of the first gas-liquid separation tank is W2, 20mm≤W2≤50mm; and / or The pitch of the second spiral guide vane is H2, the diameter of the first gas-liquid separation tank is D2, and 0.1≤H2 / D2≤1.

2.

6. The washing and dust removal purification device according to any one of claims 1 to 5, characterized in that: The washing and dust removal purification device also includes a raffinate pipe and a first circulation pump; One end of the raffinate pipe is connected to the first gas-liquid separation tank, and the other end is used to connect to the extraction device of the hydrometallurgical system, and the drain port is used to connect to the leaching device of the hydrometallurgical system; The inlet of the first circulation pump is connected to the lower part of the first gas-liquid separation tank, and the outlet of the first circulation pump is connected to the first liquid inlet pipe.

7. A roasting flue gas treatment system, characterized in that: It comprises a cooling scrubbing tower, an electrostatic precipitator and the scrubbing and dust removal purification device according to any one of claims 1 to 6, wherein the gas inlet of the cooling scrubbing tower is connected to the gas outlet pipe, and the inlet of the electrostatic precipitator is connected to the gas outlet of the cooling scrubbing tower.

8. The roasting flue gas treatment system according to claim 7, characterized in that: The roasting flue gas treatment system also includes a second circulation pump, a primary circulating water cooling heat exchanger and a secondary cryogenic heat exchanger; The inlet of the second circulation pump is connected to the liquid outlet of the cooling and washing tower, the outlet of the second circulation pump is connected to the inlet of the primary circulating water cooling heat exchanger, the outlet of the primary circulating water cooling heat exchanger is connected to the inlet of the secondary cryogenic heat exchanger, and the outlet of the secondary cryogenic heat exchanger is connected to the liquid inlet of the cooling and washing tower.

9. The roasting flue gas treatment system according to claim 7, characterized in that: The roasting fume treatment system further includes a low-temperature washing device, which is arranged between the washing and dust removal purification device and the cooling and washing tower, and includes a second washing pipe, a second connecting pipe, a second gas-liquid separation tank and a third circulation pump; One end of the second washing pipe is connected to the gas outlet pipe, and the other end is connected to the second connecting pipe. A second liquid inlet pipe is passed through the second connecting pipe. A second nozzle is provided at one end of the second liquid inlet pipe located in the second connecting pipe, and the second nozzle is arranged toward the second washing pipe. An end of the second connecting pipe away from the second washing pipe is connected to the upper part of the side wall of the second gas-liquid separation tank, the gas outlet of the second gas-liquid separation tank is connected to the gas inlet of the cooling washing tower, the inlet of the third circulating pump is connected to the liquid outlet of the second gas-liquid separation tank, and the outlet of the third circulating pump is connected to the second liquid inlet pipe.

10. The roasting flue gas treatment system according to claim 9, characterized in that: The cooling washing tower is connected to a clean water pipe; The second gas-liquid separation tank is connected to a third liquid inlet pipe, and the third liquid inlet pipe is connected to the liquid outlet of the cooling and washing tower; The first gas-liquid separation tank is connected to a fourth liquid inlet pipe, and the fourth liquid inlet pipe is connected to the outlet of the third circulation pump.

Images