Zinc sulfate recovery device during anhydrous sodium sulphate processing

Abstract

The utility model provides a zinc sulfate recovery device during anhydrous sodium sulphate processing, and relates to the technical field of zinc sulfate recovery during anhydrous sodium sulphate processing in the viscose fiber industry, supernate in a salt slurry mother solution in a roasting centrifugal machine enters an alkaline blending barrel, alkaline liquor is added into the alkaline blending barrel, zinc sulfate in the solution is converted into zinc hydroxide, and the zinc hydroxide is recycled. A zinc hydroxide solution is precipitated in the zinc removal tank, supernate in the zinc removal tank enters the roasting centrifugal machine to be continuously circulated, and zinc hydroxide precipitates in the zinc removal tank enter the acid dissolving barrel to be subjected to an acid-base reaction to generate zinc sulfate, so that zinc ions are conveniently recycled; the technical problems that in the prior art, due to the fact that zinc sulfate is contained in a spinning coagulating bath, crystallized mirabilite can contain zinc sulfate, if not treated, the crystallized mirabilite can enter the finished product anhydrous sodium sulphate, the quality of the anhydrous sodium sulphate is affected, and consumption of zinc sulfate is increased are solved.

Description

Technical Field

[0001] The utility model relates to the technical field of zinc sulfate recovery during the processing of anhydrous sodium sulfate in the viscose fiber industry, and particularly relates to a zinc sulfate recovery device during the processing of anhydrous sodium sulfate. Background Art

[0002] During the spinning and forming process of viscose fiber production, sodium sulfate is generated by the neutralization reaction of alkali in viscose with sulfuric acid. Sodium sulfate is extracted through three processes of crystallization, roasting, and drying in the acid station and processed into anhydrous sodium sulfate for sale as a by-product.

[0003] Since the spinning coagulation bath contains zinc sulfate, zinc sulfate will be carried in the crystallized mirabilite. If not treated, it will enter the finished anhydrous sodium sulfate, affecting the quality of anhydrous sodium sulfate. On the other hand, it increases the consumption of zinc sulfate. Summary of the Utility Model

[0004] The purpose of the utility model is to provide a zinc sulfate recovery device during the processing of anhydrous sodium sulfate, so as to alleviate the technical problems existing in the prior art that due to the zinc sulfate in the spinning coagulation bath, zinc sulfate will be carried in the crystallized mirabilite. If not treated, it will enter the finished anhydrous sodium sulfate, affecting the quality of anhydrous sodium sulfate and increasing the consumption of zinc sulfate.

[0005] The zinc sulfate recovery device during the processing of anhydrous sodium sulfate provided by the utility model includes: a roasting centrifuge, an alkaline preparation barrel, a zinc removal tank, and an acid dissolution barrel;

[0006] The roasting centrifuge is communicated with the alkaline preparation barrel, and the supernatant of the salt slurry mother solution in the roasting centrifuge enters the alkaline preparation barrel;

[0007] An alkaline solution is added to the alkaline preparation barrel to convert zinc sulfate in the solution into zinc hydroxide;

[0008] The alkaline preparation barrel is communicated with the zinc removal tank, and the zinc hydroxide solution in the alkaline preparation barrel enters the zinc removal tank, and the zinc removal tank is used for precipitating the zinc hydroxide solution;

[0009] The supernatant in the zinc removal tank can flow back to the roasting centrifuge;

[0010] The zinc removal tank is communicated with the acid dissolution barrel, and the zinc hydroxide precipitate in the zinc removal tank enters the acid dissolution barrel, and the acid dissolution barrel is used for causing the zinc hydroxide to undergo an acid-base reaction to generate zinc sulfate.

[0011] In an optional embodiment,

[0012] The zinc sulfate recovery device during the processing of anhydrous sodium sulfate further includes a thickening barrel;

[0013] The thickening barrel is filled with a salt slurry mother solution;

[0014] The thickening tank is communicated with the zinc removal tank, and the supernatant in the zinc removal tank can overflow into the thickening tank.

[0015] In an optional embodiment,

[0016] The sodium sulfate processing zinc sulfate recovery device further includes a suspension separator;

[0017] The suspension separator is respectively communicated with the thickening tank and the roasting centrifuge. The suspension separator is used for concentrating the salt slurry mother solution, and after concentration, it enters the roasting centrifuge, and the supernatant enters the alkaline preparation tank (200).

[0018] In an optional embodiment,

[0019] The sodium sulfate processing zinc sulfate recovery device further includes a liquid caustic soda delivery pipe;

[0020] The liquid caustic soda delivery pipe is communicated with the alkaline preparation tank, and the liquid caustic soda delivery pipe is used for delivering liquid caustic soda to the alkaline preparation tank.

[0021] In an optional embodiment,

[0022] The sodium sulfate processing zinc sulfate recovery device further includes an alkaline water delivery pump;

[0023] The alkaline water delivery pump is arranged on the communication pipeline between the alkaline preparation tank and the zinc removal tank.

[0024] In an optional embodiment,

[0025] The top of the zinc removal tank is provided with a water inlet, and the zinc hydroxide solution in the alkaline preparation tank enters the zinc removal tank through the water inlet;

[0026] The zinc removal tank is provided with packing;

[0027] The bottom of the zinc removal tank is provided with a sedimentation funnel, and the bottom opening of the sedimentation funnel is communicated with the acid dissolution tank through a sludge discharge pipeline;

[0028] The top of the zinc removal tank is provided with an overflow weir.

[0029] In an optional embodiment,

[0030] The sodium sulfate processing zinc sulfate recovery device further includes an acid bath pipeline;

[0031] The acid bath pipeline is communicated with the acid dissolution tank, and the acid bath pipeline is used for delivering acid bath into the acid dissolution tank.

[0032] In an optional embodiment,

[0033] The zinc sulfate recovery device during sodium sulfate processing further includes an acid bath bottom tank;

[0034] The acidic dissolution tank is communicated with the acid bath bottom tank, and the acidic water in the acidic dissolution tank is transported to the acid bath bottom tank through an acidic water pump.

[0035] In an alternative embodiment,

[0036] A first stirrer is arranged in the alkaline preparation tank;

[0037] A first pH meter is arranged in the alkaline preparation tank.

[0038] In an alternative embodiment,

[0039] A second stirrer is arranged in the acidic dissolution tank;

[0040] A second pH meter is arranged in the acidic dissolution tank.

[0041] For the zinc sulfate recovery device during sodium sulfate processing provided by the present utility model, the supernatant in the salt slurry mother solution in the roasting centrifuge enters the alkaline preparation tank, an alkali solution is added to the alkaline preparation tank to convert zinc sulfate in the solution into zinc hydroxide, and it is sent to the zinc removal tank. The zinc removal tank precipitates the zinc hydroxide solution, the supernatant in the zinc removal tank enters the roasting centrifuge for continuous circulation, and the zinc hydroxide precipitate in the zinc removal tank enters the acidic dissolution tank to undergo an acid-base reaction to generate zinc sulfate, which facilitates the recycling of zinc ions, and alleviates the technical problems existing in the prior art that since the spinning coagulation bath contains zinc sulfate, zinc sulfate will be carried in the crystallized mirabilite, and if not treated, it will enter the finished sodium sulfate, affecting the quality of sodium sulfate and increasing the consumption of zinc sulfate. BRIEF DESCRIPTION OF THE DRAWINGS

[0042] In order to more clearly illustrate the specific embodiments of the present utility model or the technical solutions in the prior art, the following will briefly introduce the drawings required for the description of the specific embodiments or the prior art. Obviously, the following drawings are some embodiments of the present utility model. For those of ordinary skill in the art, without creative efforts, other drawings can also be obtained based on these drawings.

[0043] Figure 1 It is a schematic diagram of the overall structure of the zinc sulfate recovery device during sodium sulfate processing provided by the embodiment of the present utility model.

[0044] Icons: 10 - caustic water transfer pump; 20 - liquid caustic transfer pipe; 30 - acid bath pipeline; 40 - acid bath bottom tank; 100 - roasting centrifuge; 200 - alkaline preparation barrel; 210 - first mixer; 220 - first pH meter; 300 - zinc removal tank; 310 - water inlet; 320 - packing; 330 - sedimentation funnel; 340 - overflow weir; 350 - sludge discharge pipeline; 400 - acid dissolution barrel; 410 - second mixer; 420 - second pH meter; 500 - thickening barrel; 600 - suspension separator. Detailed implementation manners

[0045] The technical solutions of the present utility model will be clearly and completely described below in conjunction with the accompanying drawings. Obviously, the described embodiments are some, but not all, of the embodiments of the present utility model. All other embodiments obtained by those of ordinary skill in the art based on the embodiments of the present utility model without creative efforts shall fall within the protection scope of the present utility model.

[0046] In the description of the present utility model, it should be noted that the orientation or positional relationship indicated by the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", etc. is based on the orientation or positional relationship shown in the accompanying drawings. It is only for the convenience of describing the present utility model and simplifying the description, rather than indicating or implying that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore should not be construed as a limitation of the present utility model. In addition, the terms "first", "second", and "third" are only used for descriptive purposes and cannot be construed as indicating or implying relative importance.

[0047] In the description of the present utility model, it should be noted that unless otherwise clearly defined and limited, the terms "installation", "connection", and "connection" should be understood in a broad sense. For example, it can be a fixed connection, a detachable connection, or an integral connection; it can be a mechanical connection or an electrical connection; it can be directly connected or indirectly connected through an intermediate medium, and it can be the communication inside two elements. For those of ordinary skill in the art, the specific meanings of the above terms in the present utility model can be understood according to specific situations.

[0048] The following will describe in detail the specific implementation manners of the present utility model in conjunction with the accompanying drawings. It should be understood that the specific implementation manners described herein are only used to illustrate and explain the present utility model and are not used to limit the present utility model.

[0049] As Figure 1 shown, the sodium sulfate processing zinc sulfate recovery device provided in this embodiment includes: a roasting centrifuge 100, an alkaline preparation barrel 200, a zinc removal tank 300, and an acid dissolution barrel 400.

[0050] In an alternative embodiment, the zinc sulfate recovery device during mirabilite processing further includes a thickening tank 500 and a suspension separator 600; a salt slurry mother solution is placed in the thickening tank 500, and the salt slurry mother solution in the thickening tank 500 enters the suspension separator 600, and after being concentrated by the suspension separator 600, it enters the roasting centrifuge 100, and the supernatant enters the alkaline preparation tank 200.

[0051] The roasting centrifuge 100 is connected to the alkaline preparation tank 200. After the roasting centrifuge 100 centrifuges the salt slurry mother solution, the supernatant of the salt slurry mother solution in the roasting centrifuge 100 enters the alkaline preparation tank 200.

[0052] An alkali solution is added to the alkaline preparation tank 200 to convert zinc sulfate in the solution into zinc hydroxide.

[0053] The alkaline preparation tank 200 is connected to the zinc removal tank 300. The zinc hydroxide solution in the alkaline preparation tank 200 enters the zinc removal tank 300, and the zinc removal tank 300 precipitates the zinc hydroxide solution.

[0054] The thickening tank 500 is connected to the zinc removal tank 300. The supernatant in the zinc removal tank 300 can overflow into the thickening tank 500, and the supernatant in the zinc removal tank 300 can flow back into the roasting centrifuge 100; specifically, the top of the zinc removal tank 300 is connected to the thickening tank 500, the supernatant in the zinc removal tank 300 enters the thickening tank 500, the liquid in the thickening tank 500 enters the suspension separator 600, after being concentrated by the suspension separator 600, the precipitate re-enters the roasting centrifuge 100, and the supernatant in the suspension separator 600 and the centrifuged supernatant of the roasting centrifuge 100 enter the alkaline preparation tank 200 together for subsequent neutralization precipitation process.

[0055] The zinc removal tank 300 is connected to the acid dissolution tank 400. The zinc hydroxide precipitate in the zinc removal tank 300 enters the acid dissolution tank 400, and an acid-base reaction occurs between the acid dissolution tank 400 and the zinc hydroxide to generate zinc sulfate. Specifically, an acid bath is added to the acid dissolution tank 400, and the acid bath undergoes an acid-base reaction with the zinc hydroxide precipitate. The zinc hydroxide completely reacts to generate zinc sulfate. Finally, the completely reacted acidic water is sent to the acid bath bottom tank 40 by an acid pump for zinc ion reuse.

[0056] The zinc sulfate recovery device provided in this embodiment during the processing of mirabilite. The supernatant in the salt slurry mother solution in the roasting centrifuge 100 enters the alkaline preparation tank 200. An alkali solution is added to the alkaline preparation tank 200 to convert zinc sulfate in the solution into zinc hydroxide, and then it is sent to the zinc removal tank 300. The zinc removal tank 300 precipitates the zinc hydroxide solution. The supernatant in the zinc removal tank 300 enters the roasting centrifuge 100 for continuous circulation. The zinc hydroxide precipitate in the zinc removal tank 300 enters the acidic dissolution tank 400, where an acid-base reaction occurs to generate zinc sulfate, facilitating the recycling of zinc ions and alleviating the technical problems existing in the prior art. Since the spinning coagulation bath contains zinc sulfate, zinc sulfate will be carried in the crystallized mirabilite. If not treated, it will enter the finished mirabilite, affecting the quality of mirabilite and increasing the consumption of zinc sulfate.

[0057] On the basis of the above embodiment, in an optional implementation manner, the zinc sulfate recovery device provided in this embodiment during the processing of mirabilite further includes a liquid caustic soda delivery pipe 20; the liquid caustic soda delivery pipe 20 is connected to the alkaline preparation tank 200, and the liquid caustic soda delivery pipe 20 is used to deliver liquid caustic soda to the alkaline preparation tank 200.

[0058] Specifically, one end of the liquid caustic soda delivery pipe 20 is connected to external liquid caustic soda, and the other end of the liquid caustic soda delivery pipe 20 is connected to the alkaline preparation tank 200. The liquid caustic soda is delivered to the alkaline preparation tank 200 through the liquid caustic soda delivery pipe 20.

[0059] In an optional implementation manner, the zinc sulfate recovery device during the processing of mirabilite further includes an alkaline water delivery pump 10; the alkaline water delivery pump 10 is arranged on the connecting pipeline between the alkaline preparation tank 200 and the zinc removal tank 300.

[0060] Specifically, the alkaline preparation tank 200 and the zinc removal tank 300 are connected by a pipeline. One end of the pipeline is connected to the bottom of the alkaline preparation tank 200, and the other end of the pipeline is connected to the top of the zinc removal tank 300. The solution in the alkaline preparation tank 200 enters the zinc removal tank 300 through this pipeline. The alkaline water delivery pump 10 is arranged on this pipeline to pump the solution in the alkaline preparation tank 200 into the zinc removal tank 300.

[0061] In an optional implementation manner, a water inlet 310 is arranged at the top of the zinc removal tank 300. The zinc hydroxide solution in the alkaline preparation tank 200 enters the zinc removal tank 300 through the water inlet 310. The opening of the water inlet 310 faces upward, and the solution delivered from the alkaline preparation tank 200 enters the zinc removal tank 300 from top to bottom.

[0062] Packing 320 is arranged in the zinc removal tank 300. The packing 320 can increase the effective sedimentation area for solid-liquid separation, thereby improving the sedimentation efficiency. The packing 320 is made of PP or PVC material.

[0063] A sedimentation funnel 330 is provided at the bottom of the zinc removal tank 300. Zinc hydroxide precipitates in the solution precipitate in the sedimentation funnel 330, and the bottom opening of the sedimentation funnel 330 is connected to the acidic dissolution tank 400 through a sludge discharge pipeline 350. The zinc hydroxide precipitate in the sedimentation funnel 330 flows into the acidic dissolution tank 400 through the sludge discharge pipeline 350.

[0064] An overflow weir 340 is provided at the top of the zinc removal tank 300. The supernatant in the zinc removal tank 300 enters the overflow weir 340. The overflow weir 340 is connected to the thickening tank 500. The overflow weir 340 collects the supernatant for transportation to the thickening tank 500.

[0065] In an optional embodiment, the zinc sulfate recovery device during sodium sulfate processing further includes an acid bath pipeline 30; the acid bath pipeline 30 is connected to the acidic dissolution tank 400, and the acid bath pipeline 30 transports the acid bath into the acidic dissolution tank 400.

[0066] Specifically, one end of the acid bath pipeline 30 is connected to an external acid bath, and the other end of the acid bath pipeline 30 is connected to the acidic dissolution tank 400. The acid bath enters the acidic dissolution tank 400 through the acid bath pipeline 30.

[0067] In an optional embodiment, the zinc sulfate recovery device during sodium sulfate processing further includes an acid bath bottom tank 40; the acidic dissolution tank 400 is connected to the acid bath bottom tank 40, and the acidic water in the acidic dissolution tank 400 is pumped into the acid bath bottom tank 40 through an acidic water pump for subsequent recovery of zinc ions in sodium sulfate.

[0068] In an optional embodiment, a first stirrer 210 is provided in the alkaline preparation tank 200, and the first stirrer 210 stirs the solution in the alkaline preparation tank 200; a first pH meter 220 is provided in the alkaline preparation tank 200, and the first pH meter 220 detects the pH value of the solution in the alkaline preparation tank 200.

[0069] In an optional embodiment, a second stirrer 410 is provided in the acidic dissolution tank 400, and the second stirrer 410 stirs the solution in the acidic dissolution tank 400; a second pH meter 420 is provided in the acidic dissolution tank 400, and the second pH meter 420 detects the pH value of the solution in the acidic dissolution tank 400.

[0070] The specific implementation steps are as follows:

[0071] The salt slurry mother liquor enters the thickening tank 500, is sent into the suspension separator 600 by a pump for concentration, and then enters the roasting centrifuge 100. The concentrated material enters the drying section. The supernatant is introduced into the alkaline preparation tank 200 through the feed pipe. Liquid caustic soda enters the alkaline preparation tank 200 through the liquid caustic soda delivery pipe 20. Under the action of the first stirrer, the supernatant is neutralized. A first pH meter 220 is arranged in the alkaline preparation tank 200. By means of the regulating alkali control valve on the first pH and the liquid caustic soda delivery pipe 20, the amount of alkali added is controlled. Alkali is added in the alkaline preparation tank 200 to adjust the pH value of the solution to 9 - 10, so that zinc sulfate in the solution is converted into zinc hydroxide. The zinc hydroxide enters the water inlet 310 of the zinc removal tank 300 from the alkali water delivery pump 10 through the water inlet valve. The zinc hydroxide precipitates under the action of the packing 320. The supernatant after zinc removal does not contain zinc sulfate. After passing through the packing 320, it overflows into the supernatant outlet through the overflow weir 340, and then enters the thickening tank 500 through the pipeline for continuous recycling, which can effectively reduce the zinc sulfate content in the thickening tank 500, thereby reducing the zinc sulfate content entering the roasting centrifuge 100.

[0072] The zinc hydroxide precipitated in the zinc removal tank 300 enters the sludge discharge pipeline 350 through the precipitation funnel 330 and is sent into the acid dissolution tank 400. The acid bath enters the acid dissolution tank 400 through the acid bath pipeline 30. Under the stirring of the second stirrer 410, an acid-base reaction occurs with the zinc hydroxide precipitate. A second pH meter 420 is arranged in the acid dissolution tank 400 to adjust the acid bath dosage and control the pH value at about 2, showing acidity. The zinc hydroxide reacts completely to generate zinc sulfate. Finally, the fully reacted acidic water is sent into the acid bath bottom tank 40 by the acid pump for the reuse of zinc ions.

[0073] The supernatant of the zinc precipitation tank after removing zinc ions overflows back into the thickening tank 500, thereby achieving the removal of zinc ions in the sodium sulfate.

[0074] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of the present invention, rather than to limit them; although the present invention has been described in detail with reference to the foregoing embodiments, those of ordinary skill in the art should understand that they can still modify the technical solutions described in the foregoing embodiments, or perform equivalent replacements on some or all of the technical features; and these modifications or replacements do not make the essence of the corresponding technical solutions deviate from the scope of the technical solutions of the embodiments of the present invention.

Claims

1. A zinc sulfate recovery device for glauber salt processing, characterized in that: include: A roasting centrifuge (100), an alkaline preparation tank (200), a zinc removal tank (300) and an acidic dissolution tank (400); The roasting centrifuge (100) is connected to the alkaline blending barrel (200), and the supernatant of the salt slurry mother solution in the roasting centrifuge (100) enters the alkaline blending barrel (200); Alkaline solution is added into the alkaline preparation barrel (200) to convert zinc sulfate in the solution into zinc hydroxide; The alkaline preparation barrel (200) is connected to the zinc removal tank (300), and the zinc hydroxide solution in the alkaline preparation barrel (200) enters the zinc removal tank (300), and the zinc removal tank (300) is used to precipitate the zinc hydroxide solution; The supernatant in the zinc removal tank (300) can flow back into the roasting centrifuge (100); The zinc removal tank (300) is connected to the acidic dissolution tank (400), and the zinc hydroxide precipitate in the zinc removal tank (300) enters the acidic dissolution tank (400). The acidic dissolution tank (400) is used to cause the zinc hydroxide to undergo an acid-base reaction to generate zinc sulfate.

2. The zinc sulfate recovery device during glauber salt processing according to claim 1, characterized in that: The zinc sulfate recovery device during the glauber salt processing further comprises a thickening barrel (500); The thickening barrel (500) contains a salt slurry mother solution; The thickening barrel (500) is in communication with the zinc removal tank (300), and the supernatant in the zinc removal tank (300) can overflow into the thickening barrel (500).

3. The zinc sulfate recovery device during glauber salt processing according to claim 2, characterized in that: The zinc sulfate recovery device during the glauber salt processing further comprises a suspension separator (600); The suspension separator (600) is connected to the thickening barrel (500) and the roasting centrifuge (100) respectively. The suspension separator (600) is used to concentrate the salt slurry mother solution, and after concentration, it enters the roasting centrifuge (100), and the supernatant enters the alkaline blending barrel (200).

4. The zinc sulfate recovery device during glauber salt processing according to claim 1, characterized in that: The zinc sulfate recovery device during the glauber salt processing further comprises a liquid caustic soda conveying pipe (20); The liquid caustic soda conveying pipe (20) is in communication with the alkaline preparation barrel (200), and the liquid caustic soda conveying pipe (20) is used to convey the liquid caustic soda into the alkaline preparation barrel (200).

5. The zinc sulfate recovery device during glauber salt processing according to claim 1, characterized in that: The zinc sulfate recovery device during the glauber salt processing further comprises an alkaline water delivery pump (10); The alkaline water delivery pump (10) is arranged on a connecting pipe between the alkaline preparation barrel (200) and the zinc removal pool (300).

6. The zinc sulfate recovery device during glauber salt processing according to claim 1, characterized in that: The top of the zinc removal pool (300) is provided with a water inlet (310), and the zinc hydroxide solution in the alkaline preparation barrel (200) enters the zinc removal pool (300) through the water inlet (310); A filler (320) is arranged in the zinc removal pool (300); A sedimentation funnel (330) is provided at the bottom of the zinc removal pool (300), and the bottom opening of the sedimentation funnel (330) is connected to the acidic dissolution barrel (400) through a mud discharge pipe (350); An overflow weir (340) is provided on the top of the zinc removal tank (300).

7. The zinc sulfate recovery device during glauber salt processing according to claim 1, characterized in that: The zinc sulfate recovery device during the glauber salt processing further comprises an acid bath pipeline (30); The acid bath pipeline (30) is in communication with the acid dissolution barrel (400), and the acid bath pipeline (30) is used to transport the acid bath into the acid dissolution barrel (400).

8. The zinc sulfate recovery device during glauber salt processing according to claim 1, characterized in that: The zinc sulfate recovery device during the glauber salt processing further comprises an acid bath bottom tank (40); The acid dissolution tank (400) is in communication with the acid bath bottom tank (40), and the acidic water in the acid dissolution tank (400) is transported to the acid bath bottom tank (40) by an acidic water pump.

9. The zinc sulfate recovery device during glauber salt processing according to claim 1, characterized in that: The alkaline mixing barrel (200) is provided with a first mixer (210); A first pH meter (220) is arranged in the alkaline mixing barrel (200).

10. The zinc sulfate recovery device during glauber salt processing according to claim 1, characterized in that: A second mixer (410) is provided in the acidic dissolution tank (400); A second pH meter (420) is provided in the acidic dissolution barrel (400).

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