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CN-224199502-U - Insoluble anode electrodeposition system capable of recycling byproducts

CN224199502UCN 224199502 UCN224199502 UCN 224199502UCN-224199502-U

Abstract

The utility model discloses an insoluble anode electrodeposition system capable of recycling byproducts, which comprises an electrodeposition tank unit, an oxygen collection and purification unit, an electrodeposition liquid blending and neutralization unit, a homogeneous membrane electrodialysis concentration unit, a resin purification unit and an acid-base separation unit, wherein an oxygen exhaust port is connected with an air inlet of a condenser, an anolyte overflow port is connected with an anolyte temporary storage tank, a dilute alkali circulation tank is connected with a hydroxide preparation kettle, a filtrate discharge port of a filter press is connected with a homogeneous membrane electrodialysis raw material brine feed tank, a bipolar membrane electrodialysis dilute brine temporary storage tank is connected with a raw material water feed port of a homogeneous membrane electrodialysis device, a homogeneous membrane electrodialysis concentrated brine temporary storage tank is connected with a feed port of a multi-stage resin exchange tower, a dilute acid circulation tank is connected with a feed port of a multi-stage resin exchange tower, and a purified concentrated brine storage tank is connected with a raw material brine feed port of a bipolar membrane electrodialysis device. The utility model can recycle byproducts in the sulfate system insoluble anode electro-deposition process, has good effect and lower input cost.

Inventors

  • LIU ZHAN
  • ZHANG MINGYING
  • LIU LINXUE
  • LIU GUANGHAN

Assignees

  • 浙江聚泰新能源材料有限公司
  • 陕西聚泰新材料科技有限公司

Dates

Publication Date
20260505
Application Date
20250507

Claims (10)

  1. 1. The insoluble anode electrodeposition system capable of recycling byproducts comprises an electrodeposition tank unit (1), wherein the electrodeposition tank unit (1) comprises an electrodeposition tank body (101), a plurality of anode areas (14) and cathode areas (15) which are alternately distributed in the electrodeposition tank body (101), anodes are arranged in each anode area (14), an anode exhaust port (103) and an anolyte overflow port (104) are arranged in each anode area (14), the anolyte overflow ports (104) are arranged on the electrodeposition tank body (101), a diaphragm bag is hung in each cathode area (15), a cathode piece extending into the diaphragm bag is arranged in each cathode area (15), and the cathode areas (15) are connected with an electrodeposition tank electrolyte feed port (105); The method is characterized in that: The insoluble anode electro-deposition system capable of recycling byproducts also comprises an oxygen collection and purification unit (2), an electro-deposition liquid allocation and neutralization unit (3), a homogeneous membrane electrodialysis concentration unit (4), a resin purification unit (5) and an acid-base separation unit (6); The oxygen collection and purification unit (2) comprises a condenser (201), and a gas outlet after top condensation of the condenser (201) is connected with an oxygen storage tank (202); The electro-deposition solution preparation and neutralization unit (3) comprises an anode solution temporary storage tank (301), the anode solution temporary storage tank (301) is connected with an electro-deposition solution preparation and neutralization kettle (302), a hydroxide charging port of the electro-deposition solution preparation and neutralization kettle (302) is connected with a filter cake discharging and walking groove of a filter press (303), and a charging port of the filter press (303) is connected with a hydroxide preparation kettle (304); The homogeneous membrane electrodialysis concentration unit (4) comprises a homogeneous membrane electrodialysis raw material brine feed tank (401), wherein the homogeneous membrane electrodialysis raw material brine feed tank (401) is connected with a raw material brine feed inlet of the homogeneous membrane electrodialysis device (402), and a concentrated brine discharge outlet of the homogeneous membrane electrodialysis device (402) is connected with a homogeneous membrane electrodialysis concentrated brine temporary storage tank (403); The resin purifying unit (5) comprises a plurality of stages of resin exchange towers (501), the discharge ports of the plurality of stages of resin exchange towers (501) are connected with a purified strong brine storage tank (502), The acid-base separation unit (6) comprises a bipolar membrane electrodialysis device (601), wherein a dilute brine discharge port of the bipolar membrane electrodialysis device (601) is connected with a dilute brine temporary storage tank (602) of the bipolar membrane electrodialysis device, a dilute alkali circulation discharge port of the bipolar membrane electrodialysis device (601) is connected with a feed port of a dilute alkali circulation tank (603), and a discharge port of the dilute alkali circulation tank (603) is connected with a dilute alkali circulation feed port of the bipolar membrane electrodialysis device (601) to realize dilute alkali circulation; The discharge port of the electro-deposition liquid neutralization and preparation kettle (302) is connected with the feed port of the electro-deposition liquid high-level tank (106), and the bottom discharge port of the electro-deposition liquid high-level tank (106) is connected with the electro-deposition liquid feed port (105) of the electro-deposition tank to provide electro-deposition liquid; The anode exhaust port (103) is connected with the air inlet of the condenser (201); The anolyte overflow port (104) is connected with the anolyte temporary storage tank (301), and the dilute alkali circulation tank (603) is connected with the hydroxide preparation kettle (304); The filtrate outlet of the filter press (303) is connected with the homogeneous membrane electrodialysis raw material brine feed tank (401), and the bipolar membrane electrodialysis fresh brine temporary storage tank (602) is connected with the raw material water feed inlet of the homogeneous membrane electrodialysis device (402); The homogeneous membrane electrodialysis strong brine temporary storage tank (403) is connected with the feed inlet of the multi-stage resin exchange tower (501), and the dilute acid circulation tank (604) is connected with the feed inlet of the multi-stage resin exchange tower (501); The purified strong brine storage tank (502) is connected with a raw brine feed inlet of the bipolar membrane electrodialysis device (601).
  2. 2. The insoluble anode electrodeposition system of claim 1, wherein a top feed port of said high level tank (106) is connected to a discharge port of a first filter (307), and a feed port of said first filter (307) is connected to a discharge port of said neutralization and formulation tank (302) for continuous feeding.
  3. 3. The insoluble anode electrodeposition system as in claim 1, wherein in the oxygen collection and purification unit (2), a condensate outlet at the bottom of the condenser (201) is connected to the condensate temporary storage tank (203), a gas outlet after top condensation of the condenser (201) is connected to the buffer tank (204), the buffer tank (204) is connected to the concentrated sulfuric acid drying tank (205), the concentrated sulfuric acid drying tank (205) is connected to the compressor (206) via a check valve, and the compressor (206) is connected to the oxygen storage tank (202).
  4. 4. The insoluble anode electrodeposition system of recoverable byproducts as described in claim 1, wherein in said electrodeposition liquid blending and neutralization unit (3), the feed inlet of the filter press (303) is further connected to a pure water pipe (13), the filtrate discharge outlet of said filter press (303) is connected to a filtrate temporary storage tank (305), the filtrate temporary storage tank (305) is connected to the feed inlet of a second filter (306), and the discharge outlet of the second filter (306) is connected to a feed tank (401) for the homogeneous membrane electrodialysis raw material brine.
  5. 5. The insoluble anode electrodeposition system of recoverable byproducts according to claim 1, wherein in said homogeneous membrane electrodialysis concentration unit (4), the dilute brine feed inlet of the homogeneous membrane electrodialysis device (402) is connected to a homogeneous membrane electrodialysis dilute brine temporary storage tank (404), and the homogeneous membrane electrodialysis dilute brine temporary storage tank (404) is connected to a pure water preparation pipeline (405).
  6. 6. The insoluble anode electrodeposition system according to claim 1, wherein in the resin purifying unit (5), the feed ports of the resin exchange columns (501) of the plurality of stages are connected to the compressed air pipe (503), and the discharge port of the resin exchange column (501) of the upper stage is connected to the feed port of the resin exchange column (501) of the next stage.
  7. 7. The insoluble anode electrodeposition system of recoverable byproducts according to claim 1, wherein in said acid-base separation unit (6), a polar water circulation discharge port of a bipolar membrane electrodialysis device (601) is connected with a feed port of a polar water circulation tank (605), and a discharge port of the polar water circulation tank (605) is connected with a polar water circulation feed port of said bipolar membrane electrodialysis device (601) to realize polar water circulation, said polar water circulation tank (605) is also connected with a bipolar membrane electrodialysis fresh brine temporary storage tank (602); The polar water circulation discharge port of the bipolar membrane electrodialysis device (601) is also connected with a pure water pipeline (13) for supplementing water, the dilute alkali circulation tank (603) is also connected with the pure water pipeline (13) for supplementing water, and the dilute acid circulation tank (604) is also connected with the pure water pipeline (13) for supplementing water; The dilute alkali circulating tank (603) is connected with the hydroxide preparation kettle (304) through a check valve, and the dilute acid circulating tank (604) is connected with the feed inlet of the multistage resin exchange tower (501) through a check valve; The top of the polar water circulation tank (605) is also provided with a flame arrester (606).
  8. 8. The insoluble anode electrodeposition system according to claim 1, wherein the electrodeposition cell body (101) is provided with a cell interior member assembly (102), and the cell interior member assembly (102) is provided with an anode exhaust port (103) and an electrodeposition cell electrolyte feed port (105).
  9. 9. The insoluble anode electrowinning system as claimed in claim 8, wherein said tank trim assembly (102) includes a tank panel (10201), said tank panel (10201) having an anode exhaust port (103) and an electrowinning tank electrolyte feed port (105) disposed on a vertical top surface thereof; The groove panel (10201) is provided with a plurality of anode positioning strip-shaped holes (10202) and a plurality of cathode positioning strip-shaped holes (10203) which are uniformly and alternately distributed in a transverse direction, the length directions of the anode positioning strip-shaped holes (10202) and the cathode positioning strip-shaped holes (10203) are distributed along the longitudinal direction, and the width directions of the anode positioning strip-shaped holes (10202) and the cathode positioning strip-shaped holes (10203) are distributed along the transverse direction; A circle of reinforcing ribs (10204) are arranged on the edge of the vertical bottom surface of the groove panel (10201), a cathode cloth total channel (10205) is arranged in the reinforcing ribs (10204), the feeding end of the cathode cloth total channel (10205) is communicated with the electro-deposition groove electro-deposition liquid feeding port (105), and the discharging side of the cathode cloth total channel (10205) is also communicated with a plurality of cathode cloth sub-channels (10206) arranged in the reinforcing ribs (10204); A circle of cathode coaming plates (10207) are arranged on the vertical bottom surface of the groove panel (10201) around each cathode positioning strip-shaped hole (10203), material distribution overflow grooves (10208) are arranged on the vertical side walls of the cathode coamings (10207) close to the cathode positioning strip-shaped holes (10203), and the material distribution overflow grooves (10208) are communicated with the cathode material distribution sub-channels (10206) in a one-to-one correspondence manner; A diaphragm bag hook (10209) is arranged on the vertical side wall of the cathode coaming (10207) below the cloth overflow groove (10208), and a diaphragm frame (10210) is fixedly arranged at the vertical bottom of the cathode coaming (10207), a diaphragm bag is arranged in the diaphragm frame (10210), and the top of the diaphragm bag is hung on the diaphragm bag hook (10209); The groove panel (10201) is also provided with an anode exhaust channel (10211), and the anode exhaust channel (10211) is connected with the anode exhaust port (103).
  10. 10. The insoluble anode electrodeposition system according to claim 9, wherein the diaphragm frame (10210) has an external dimension of 800 to 1200mm in length and width, a mesh of Fang Xingge, a square of 80 to 120mm x (80 to 120 mm), and a rim of Fang Xingge of 8 to 12mm x (8 to 12 mm) and has the same length and width as the cathode cover plate.

Description

Insoluble anode electrodeposition system capable of recycling byproducts Technical Field The utility model belongs to the technical field of nonferrous metals, relates to insoluble anode metal electrodeposition, and in particular relates to an insoluble anode electrodeposition system capable of recycling byproducts. Background In the insoluble anodic electrodeposition process of sulfate systems, the prior art often only pays attention to the main product metal plate, and the byproducts are ignored or not recycled. The sulfate system insoluble anode electrodeposition byproducts mainly comprise oxygen and sulfuric acid generated by an anode, and the method of emptying and neutralizing is simply adopted by manufacturers in a scale of hours to meet the electrodeposition process, but the significance of recycling the oxygen and the sulfuric acid is great if the scale is large. In a production workshop for electrodepositing nickel in 1 ten thousand tons/year, 2726.2 tons of oxygen and 16698 tons of sulfuric acid can be theoretically produced each year, 1000 ten thousand RMB are conservatively estimated, only a tail gas induced draft fan consumes about 60 ten thousand degrees each year according to the acid and salt mist treatment process carried out by the existing emptying oxygen, and 18061 tons of sodium carbonate (about 4515 RMB in value) are consumed each year in the existing process for neutralizing sulfuric acid, so that the corresponding equipment investment and running cost are not considered. The existing technology is not exactly to treat the byproducts, which not only consumes great cost, but also generates new pollution, such as the neutralization of sodium carbonate, 7497 tons of carbon dioxide are directly discharged each year, 241950 tons of high-salt wastewater (10 percent content) is generated, and 24195 tons of waste sodium sulfate is generated as a byproduct. The existing technology for treating the acid and salt mist carried out by the anode oxygen does not recycle the acid and salt mist as a byproduct, but only treats the acid and salt mist from the aspects of environmental protection and site occupational health, and has poor effect and high treatment cost. How to recover all the produced products while the electro-winning can be performed with high efficiency is an important subject to be put in front of the scientific workers engaged in the hydrometallurgical field. From the above analysis, it is not only necessary to change the overall sulfate system insoluble anodic electrodeposition system and process but also to modify the conventional electrodeposition cell and ancillary equipment, which can be perfectly solved only if the equipment and process system are closely matched. That is, the three blocks of the traditional technology, namely an electrowinning tank system, a tail gas treatment system, an electrowinning tank feeding and anode discharging electrowinning liquid treatment system, are fundamentally changed. Regarding the process parameters of the electrowinning cell system, which are not changed, how the electrowinning cell is opened and the oxygen discharged from the anode can be collected becomes the key of the problem, the traditional electrowinning cell system is that different manufacturers respectively produce the electrowinning cell and cell internals (comprising a diaphragm frame, a feeder, a mist collecting cover, a diaphragm bag, a bag supporting device, corresponding fixing pieces and the like) and then the electrowinning cell system is transported to site installation and site location. The method has the advantages that the processing precision of products, the precision after installation and the sealing can not be guaranteed due to the fact that the assembly parts are produced by different manufacturers, the high-quality recovery of oxygen can not be guaranteed due to the fact that the efficiency of electrodeposition and the on-site automation operation are greatly influenced, therefore, the novel electrodeposition tank system is designed and produced, the novel problem of the electrodeposition tank production design can be solved, the method can be used for accurately operating the electrodeposition process and the on-site automation operation, the oxygen generated by an anode can be collected, if the anode oxygen can be effectively collected, the tail gas treatment system is easy to increase, the oxygen purification process is actually changed, the problems are simple and the energy consumption is greatly reduced, the problem about sulfuric acid recovery is relatively complex, sulfuric acid in an anodic electrolyte generally contains 15-50 g/L, lei Junpeng and the like, the diffusion dialysis method reported by P40-P42 in the 5 th coil of the "nonferrous metal engineering" P40-P42 in 2017 "can be used for separating and researching nickel-electro-deposition anode acid salt, sulfuric acid in the solution can be recovered, the sulfuric acid in 80% is 80%, the sulfur