Production device of polymeric ferric chloride sulfate

Abstract

The utility model discloses a production device of polymeric ferric chloride sulfate, which comprises a pressure-resistant tank body, a main / auxiliary liquid inlet pipe orifice, an exhaust pipe orifice and an upper gas inlet pipe orifice are arranged at the top of the pressure-resistant tank body, a liquid outlet pipe orifice is arranged at the bottom of the pressure-resistant tank body, and three lower gas inlet pipe orifices are uniformly distributed in the circumferential direction of the tank body; the main ejector is connected with a main liquid inlet pipe opening and exhausts circularly, and the auxiliary ejector injects liquid into the position below the liquid level through an extension pipe. According to the utility model, the design of an under-liquid gas distribution pipe is canceled, and a three-dimensional gas supply layout is adopted, so that the problems that the traditional structure is easy to corrode and perforate and the gas distribution is non-uniform are solved; the lower gas inlet pipe opening and the upper gas inlet pipe opening which are circumferentially symmetrical form a spiral gas-liquid mixed flow, the gas diffusion uniformity is improved, and oxidation dead angles are reduced; the main ejector and the auxiliary ejector work cooperatively, the long throat structure of the main ejector strengthens turbulent mixing, the short throat design of the auxiliary ejector generates deep microbubbles, the gas-liquid contact area is increased, and the reaction efficiency is improved; the oxygen distribution proportion and the injection mode can be flexibly adjusted to adapt to the raw material concentration fluctuation of + / -20%.

Description

Technical Field

[0001] This utility model relates to the field of waste acid recycling and treatment technology, specifically to a production device for polyferric chloride sulfate. Background Technology

[0002] For industrial and wastewater treatment applications, the production processes for polyferric sulfate, ferric chloride, and similar products are largely consistent with traditional pickling processes. Therefore, it is possible to treat and dispose of pickling wastewater from the steel industry using appropriate processes to produce polyferric sulfate or ferric chloride and other related iron salt flocculants that meet the quality standards of specific application areas. This process achieves the harmless treatment of pickling wastewater and enables the secondary utilization of waste acid. The above methods can effectively reduce resource waste and environmental pollution, and provide high-quality products that meet the requirements of specific fields.

[0003] Patent document CN215028722U discloses a waste acid treatment reactor that uses an annular gas distribution pipe extending into the liquid surface. This reactor has the following drawbacks: (1) the gas distribution pipe is easily pitted and perforated due to long-term immersion in acidic liquid; (2) the gas pores of the gas distribution pipe are easily blocked, requiring frequent shutdowns for cleaning; (3) the gas distribution at the far end of the gas distribution pipe is uneven, with localized oxidation dead zones. Furthermore, this reactor uses a single-stage injector, which limits its adaptability and ability to meet the production needs of different batches of products. Utility Model Content

[0004] In order to overcome the shortcomings of existing equipment for preparing polyferric chloride using pickling waste liquid, this utility model provides a production device for polyferric chloride.

[0005] The technical solution adopted in this utility model is as follows: A production device for polyferric chloride, comprising: a pressure-resistant tank, with a main liquid inlet, a main exhaust outlet, a secondary liquid inlet, a secondary exhaust outlet and an upper air inlet at the top of the tank, a liquid outlet at the bottom of the tank, and three lower air inlets arranged circumferentially around the tank body; a main injector, with a liquid inlet section connected to a liquid supply pump, an air inlet section connected to the main exhaust outlet, and a liquid outlet section installed at the main liquid inlet; and a secondary injector, with a liquid inlet section connected to a liquid supply pump, an air inlet section connected to the secondary exhaust outlet, and a liquid outlet section installed at the secondary liquid inlet.

[0006] Preferably, the three lower air inlets are located at the same height, and the included angle between adjacent lower air inlets is 120°.

[0007] Preferably, the flow rate of the main injector is greater than that of the auxiliary injector, and the auxiliary inlet pipe is connected to an extension pipe, the end of which is located 1 / 4 to 1 / 3 of the tank height below the liquid surface.

[0008] Preferably, the nozzle throat length of the main injector is 1.2-1.5 times its diameter, and the nozzle throat length of the auxiliary injector is 0.8-1 times its diameter.

[0009] Preferably, the main injector and the auxiliary injector are equipped with independent liquid supply pumps, or are connected to the same liquid supply pump and controlled by a reversing valve.

[0010] Preferably, the pressure tank body is provided with a first manhole, a temperature port and a pressure port on the top of the tank.

[0011] Preferably, a second manhole is provided on the top and bottom of the pressure tank, and the second manhole is a structure with a pressurized bolt connection.

[0012] Preferably, the oxygen distribution ratio between the upper air inlet and the lower air inlet is 10-30% for the upper inlet and 70-90% for the lower inlet.

[0013] This utility model has the following beneficial effects:

[0014] 1. Improved structural reliability: The design of the submerged gas distribution pipe was eliminated, and a combination of circumferentially distributed gas inlets on the lower part of the tank wall and gas inlets on the top was adopted to completely solve the pitting and perforation problems of the traditional annular gas distribution pipe.

[0015] 2. Gas distribution optimization: Three sets of 120° symmetrically distributed lower air inlets, combined with the top single-point air inlet three-dimensional air supply layout, form a spiral rising gas-liquid mixing flow. Actual measurements show that the uniformity of gas diffusion is significantly improved, the dead zone area of ​​oxidation reaction is reduced, and full-dimensional oxidation coverage of the reaction system is achieved.

[0016] 3. Synergistic effect of dual-stage injection: The staged design of the main and auxiliary injectors breaks through the flow limit of single-stage injection. The main injector adopts a long throat structure to achieve high-speed jet, which drives strong turbulence in the upper part of the tank. The auxiliary injector injects the reaction liquid into the liquid surface through the extension tube, and forms a deep microbubble group with the short throat nozzle. The dual-stage synergy increases the gas-liquid contact area and shortens the reaction time.

[0017] 4. Anti-clogging and self-cleaning function: All air inlets adopt a straight-through structure, which, together with the negative pressure ejection effect generated by the injector, forms a high-speed airflow of 10-15m / s to scour, improving the anti-clogging performance compared with traditional air distribution pipe systems;

[0018] 5. Flexible production control: The independent pump control scheme for the main and auxiliary injectors can realize the dual-injection full-power high-production mode, the main injection single-action maintenance mode, and the auxiliary injection compensation and adjustment mode. With the adjustable oxygen distribution ratio, it can adapt to the production needs of raw material acid concentration fluctuations of ±20%.

[0019] 6. Safety and ease of maintenance: The double-layer manhole design, combined with online monitoring of pressure and temperature ports, enables maintenance operations while ensuring safe maintenance. Attached Figure Description

[0020] Figure 1 This is a schematic diagram of an embodiment of the present utility model.

[0021] Figure 2 This is a schematic diagram of the pipe opening according to an embodiment of the present invention.

[0022] Pressure tank 1, main liquid inlet N1, main exhaust pipe N2, auxiliary liquid inlet N3, auxiliary exhaust pipe N4, upper air inlet N5, liquid outlet N6, lower air inlet N7, N8, N9, first manhole N10, second manhole N11, temperature port T, pressure port P;

[0023] Main injector 2;

[0024] Sub-injector 3;

[0025] Extension tube 4. Detailed Implementation

[0026] The present invention will be further described below with reference to the embodiments and accompanying drawings.

[0027] In the embodiments, such as Figure 1 , Figure 2 The diagram shows a production apparatus for polyferric chloride, comprising: a pressure tank 1, with a main liquid inlet N1, a main exhaust pipe N2, a secondary liquid inlet N3, a secondary exhaust pipe N4, and an upper air inlet N5 at the top; a liquid outlet N6 at the bottom; and three lower air inlets N7, N8, and N9 arranged circumferentially around the tank body; a main injector 2, with its liquid inlet section connected to a liquid supply pump, its air inlet section connected to the main exhaust pipe N2, and its liquid outlet section installed at the main liquid inlet N1; and a secondary injector 3, with its liquid inlet section connected to a liquid supply pump, its air inlet section connected to the secondary exhaust pipe N4, and its liquid outlet section installed at the secondary liquid inlet N3. This embodiment eliminates the need for a submerged gas distribution pipe design, employing a combined gas supply method with circumferentially distributed lower air inlets N7, N8, and N9 on the tank wall and an upper air inlet N5 at the top, completely solving the pitting and perforation problems inherent in traditional annular gas distribution pipes.

[0028] In the embodiments, such as Figure 1 , Figure 2 As shown, the three lower air inlets N7, N8, and N9 are located at the same height, and the angle between adjacent lower air inlets N7, N8, and N9 is 120°. Moreover, the oxygen distribution ratio between the upper air inlet N5 and the lower air inlets N7, N8, and N9 is 10-30% for the upper inlet and 70-90% for the lower inlet. The three sets of symmetrically distributed lower air inlets N7, N8, and N9 at 120° angles, combined with the three-dimensional air supply layout of the single-point upper air inlet N5 at the top, form a spiral upward gas-liquid mixing flow. Actual measurements show that the gas diffusion uniformity is significantly improved, the dead zone area of ​​the oxidation reaction is reduced, and full-dimensional oxidation coverage of the reaction system is achieved.

[0029] In the embodiments, such as Figure 1 , Figure 2 As shown, the flow rate of the main injector 2 is greater than that of the auxiliary injector 3, and the auxiliary inlet pipe N3 is connected to an extension pipe 4, the end of which is located 1 / 4 to 1 / 3 of the tank height below the liquid surface. Furthermore, the nozzle throat length of the main injector 2 is 1.2 to 1.5 times its diameter, while the nozzle throat length of the auxiliary injector 3 is 0.8 to 1 times its diameter. The main injector 2 and the auxiliary injector 3 are equipped with independent liquid supply pumps, or connected to the same liquid supply pump and controlled by a reversing valve. This staged design of the main and auxiliary injectors overcomes the flow rate limitations of single-stage injection. The main injector 2 uses a long throat structure to achieve high-speed jets, driving strong turbulence in the upper part of the tank. The auxiliary injector 3 injects the reaction liquid below the liquid surface through the extension pipe 4, forming a deep microbubble cluster with the short-throat nozzle. This dual-stage synergy increases the gas-liquid contact area and shortens the reaction time. The independent pump control scheme for the main and auxiliary injectors can realize the dual-injection full-power high-production mode, the main injection single-action maintenance mode, and the auxiliary injection compensation and adjustment mode. With the adjustable oxygen distribution ratio, it can adapt to the production needs of raw material acid concentration fluctuations of ±20%, and achieve the purpose of flexible production control.

[0030] In the embodiments, such as Figure 1 , Figure 2 As shown, the pressure tank 1 has a first manhole N10, a temperature port T, and a pressure port P on its top; a second manhole N11 is located on the bottom of the top of the pressure tank 1, and the second manhole N11 has a pressurized bolt connection structure. This double-layer manhole design, combined with online monitoring of the pressure port P and temperature port T, enables maintenance operations while ensuring safe maintenance. Remote sensors are installed at the temperature port T and pressure port P, facilitating automated control of the equipment.

[0031] Obviously, the above embodiments of this utility model are merely examples for illustrating the present utility model, and are not intended to limit the implementation of the present utility model. Other obvious variations or modifications derived from the essential spirit of the present utility model still fall within the protection scope of the present utility model.

Claims

1. An apparatus for producing polymeric ferric sulfate chloride, characterized by comprising: The application relates to a pressure-resistant tank body (1) and a main injector (2) and a secondary injector (3) arranged in the tank body (1). The tank body (1) is provided with a main liquid inlet pipe (N1), a main exhaust pipe (N2), a secondary liquid inlet pipe (N3), a secondary exhaust pipe (N4) and an upper gas inlet pipe (N5) on the tank top, and a liquid outlet pipe (N6) on the tank bottom, and three lower gas inlet pipes (N7, N8, N9) are arranged on the tank body periphery. The main injector (2) is connected with a liquid supply pump in the liquid inlet section, is communicated with the main exhaust pipe (N2) in the gas inlet section, and is installed on the main liquid inlet pipe (N1) in the liquid outlet section. The secondary injector (3) is connected with a liquid supply pump in the liquid inlet section, is communicated with the secondary exhaust pipe (N4) in the gas inlet section, and is installed on the secondary liquid inlet pipe (N3) in the liquid outlet section.

2. The apparatus for producing polyaluminum ferric sulfate according to claim 1, wherein The three lower gas inlet pipes (N7, N8, N9) are located at the same height, and the included angle between adjacent lower gas inlet pipes (N7, N8, N9) is 120 DEG.

3. The production apparatus of polymeric ferric sulfate of claim 1, wherein, The flow of the main injector (2) is greater than that of the secondary injector (3), and an extension pipe (4) is connected to the secondary liquid inlet pipe (N3), and the end of the extension pipe (4) is located below the liquid surface by 1 / 4-1 / 3 of the tank body height.

4. The apparatus for producing polyaluminum ferric sulfate of claim 1 or 3, wherein The nozzle throat length of the main injector (2) is 1.2-1.5 times of the diameter, and the nozzle throat length of the secondary injector (3) is 0.8-1 times of the diameter.

5. The apparatus for producing polyaluminum ferric sulfate of claim 1 or 3, wherein The main injector (2) and the secondary injector (3) are provided with independent liquid supply pumps, or are connected with the same liquid supply pump and are controlled through a reversing valve.

6. The production apparatus of polymeric ferric sulfate of claim 1, wherein, The tank top of the pressure-resistant tank body (1) is provided with a first manhole (N10), a temperature port (T) and a pressure port (P).

7. The production apparatus of polymeric ferric sulfate of claim 1, wherein The tank top of the pressure-resistant tank body (1) is provided with a second manhole (N11), and the second manhole (N11) is a bolted connection structure under pressure.

8. The production apparatus of polymeric ferric sulfate of claim 1, wherein, The oxygen distribution ratio of the upper gas inlet pipe (N5) to the lower gas inlet pipes (N7, N8, N9) is 10-30% for the upper and 70-90% for the lower.

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