CN221579727U - Electronic aluminum foil waste sulfuric acid low-temperature normal-pressure evaporation crystallization recovery device - Google Patents
Electronic aluminum foil waste sulfuric acid low-temperature normal-pressure evaporation crystallization recovery device Download PDFInfo
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- CN221579727U CN221579727U CN202323606867.5U CN202323606867U CN221579727U CN 221579727 U CN221579727 U CN 221579727U CN 202323606867 U CN202323606867 U CN 202323606867U CN 221579727 U CN221579727 U CN 221579727U
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- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 title claims abstract description 84
- 238000001704 evaporation Methods 0.000 title claims abstract description 82
- 230000008020 evaporation Effects 0.000 title claims abstract description 79
- 239000002699 waste material Substances 0.000 title claims abstract description 51
- 238000002425 crystallisation Methods 0.000 title claims abstract description 43
- 230000008025 crystallization Effects 0.000 title claims abstract description 41
- 229910052782 aluminium Inorganic materials 0.000 title claims abstract description 36
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 title claims abstract description 34
- 239000011888 foil Substances 0.000 title claims abstract description 31
- 238000011084 recovery Methods 0.000 title claims abstract description 25
- 239000002253 acid Substances 0.000 claims abstract description 77
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 26
- 238000007710 freezing Methods 0.000 claims abstract description 22
- 239000000945 filler Substances 0.000 claims abstract description 12
- 238000009826 distribution Methods 0.000 claims abstract description 10
- 230000008014 freezing Effects 0.000 claims description 20
- 238000004064 recycling Methods 0.000 claims description 17
- 238000007599 discharging Methods 0.000 claims description 10
- 239000012452 mother liquor Substances 0.000 claims description 10
- 238000009833 condensation Methods 0.000 claims description 7
- 230000005494 condensation Effects 0.000 claims description 7
- 239000007788 liquid Substances 0.000 description 19
- 238000000034 method Methods 0.000 description 12
- 238000004519 manufacturing process Methods 0.000 description 9
- 230000008569 process Effects 0.000 description 9
- 238000000502 dialysis Methods 0.000 description 8
- 238000009792 diffusion process Methods 0.000 description 7
- 239000012528 membrane Substances 0.000 description 7
- 239000013078 crystal Substances 0.000 description 6
- 229920006395 saturated elastomer Polymers 0.000 description 6
- 238000000926 separation method Methods 0.000 description 6
- 238000001816 cooling Methods 0.000 description 5
- 238000005260 corrosion Methods 0.000 description 5
- 230000007797 corrosion Effects 0.000 description 5
- 239000002994 raw material Substances 0.000 description 5
- 238000012546 transfer Methods 0.000 description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 4
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 4
- 239000006260 foam Substances 0.000 description 4
- 229910002804 graphite Inorganic materials 0.000 description 4
- 239000010439 graphite Substances 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- 238000006386 neutralization reaction Methods 0.000 description 4
- -1 aluminum ions Chemical class 0.000 description 3
- ZJOKNSFTHAWVKK-UHFFFAOYSA-K aluminum octadecanoate sulfate Chemical compound C(CCCCCCCCCCCCCCCCC)(=O)[O-].[Al+3].S(=O)(=O)([O-])[O-] ZJOKNSFTHAWVKK-UHFFFAOYSA-K 0.000 description 3
- 239000002585 base Substances 0.000 description 3
- 238000005530 etching Methods 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 150000003839 salts Chemical class 0.000 description 3
- 239000002893 slag Substances 0.000 description 3
- 239000002002 slurry Substances 0.000 description 3
- 238000005406 washing Methods 0.000 description 3
- KXGFMDJXCMQABM-UHFFFAOYSA-N 2-methoxy-6-methylphenol Chemical compound [CH]OC1=CC=CC([CH])=C1O KXGFMDJXCMQABM-UHFFFAOYSA-N 0.000 description 2
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 2
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 2
- 235000011941 Tilia x europaea Nutrition 0.000 description 2
- 230000032683 aging Effects 0.000 description 2
- 239000003513 alkali Substances 0.000 description 2
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 2
- 239000003990 capacitor Substances 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000000706 filtrate Substances 0.000 description 2
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 2
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 2
- 239000004571 lime Substances 0.000 description 2
- 229920001568 phenolic resin Polymers 0.000 description 2
- 239000005011 phenolic resin Substances 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 239000012629 purifying agent Substances 0.000 description 2
- 235000011149 sulphuric acid Nutrition 0.000 description 2
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 1
- 239000004743 Polypropylene Substances 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- DIZPMCHEQGEION-UHFFFAOYSA-H aluminium sulfate (anhydrous) Chemical compound [Al+3].[Al+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O DIZPMCHEQGEION-UHFFFAOYSA-H 0.000 description 1
- AMVQGJHFDJVOOB-UHFFFAOYSA-H aluminium sulfate octadecahydrate Chemical compound O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.[Al+3].[Al+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O AMVQGJHFDJVOOB-UHFFFAOYSA-H 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
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- 238000011161 development Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000003631 expected effect Effects 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 239000007770 graphite material Substances 0.000 description 1
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 229910017604 nitric acid Inorganic materials 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 229920001155 polypropylene Polymers 0.000 description 1
- 238000003825 pressing Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000009270 solid waste treatment Methods 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 239000008399 tap water Substances 0.000 description 1
- 235000020679 tap water Nutrition 0.000 description 1
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- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The utility model discloses an electronic aluminum foil waste sulfuric acid low-temperature normal-pressure evaporation crystallization recovery device, which comprises an evaporation tower, wherein one side of the lower end of the evaporation tower is sequentially connected with an acid inlet secondary preheater, an acid inlet preheater and an acid inlet pump; the other side of the lower end of the evaporation tower is sequentially connected with a medium circulating pump, a preheater and a steam heat exchanger, and the steam heat exchanger is connected with the top of the evaporation tower through a connecting pipe to form a circulating loop. The evaporator is characterized in that a demister, a water distribution system and a filler are sequentially arranged in the evaporator from top to bottom. The lower part of the evaporation tower is connected with a centrifugal fan through a pipeline, and the centrifugal fan blows cold dry air into the evaporation tower. The utility model uses AFC normal pressure evaporation-freezing crystallization method to carry out evaporation crystallization recovery to the waste sulfuric acid of the electronic aluminum foil. The device consists of two independent units of an AFC evaporation system and a freeze crystallization system, and forms a complete evaporation crystallization recovery process.
Description
Technical Field
The utility model relates to the technical field of crystallization recovery, in particular to a low-temperature normal-pressure evaporation crystallization recovery device for waste sulfuric acid of an electronic aluminum foil.
Background
The aluminum foil is used as a key raw material for manufacturing the aluminum electrolytic capacitor, is a high added value product, and is a novel electronic functional material for encouraging and supporting development. However, the aluminum foil production process has typical characteristics of high consumption and high pollution, and mainly comprises two working procedures of corrosion and formation. The etching process is a key process link for obtaining the aluminum electrolytic capacitor with excellent performance, and orderly etching pits are formed on the surface of the aluminum foil through the action of etching liquid (H 2SO4、HNO3, HCl and mixed acid thereof) so as to increase the capacitance of the material. In the corrosion process, the continuous accumulation of aluminum ions causes that the acid liquor can not meet the process requirements. At this time, part of the aging liquid needs to be replaced by new liquid, and the replaced aging liquid is mixed to form waste acid.
The current treatment mode mainly comprises an acid-base neutralization and diffusion dialysis membrane recycling method. The two treatment processes have the following disadvantages:
1. The acid-base neutralization method directly causes the waste of sulfuric acid resources in waste acid, and all sulfuric acid reacts with lime to generate waste residue (calcium sulfate) which cannot be recycled.
2. Acid-base neutralization treatment is adopted, a large amount of neutralization raw material lime is purchased, and the generated waste slag is too large, so that the waste slag solid waste treatment cost is high. Meanwhile, the slag slurry is required to be separated by matching filter pressing equipment, and the treatment cost is high.
3. When the diffusion dialysis membrane is used for treating waste acid, the membrane performance, the waste liquid composition and the operation parameters of the diffusion dialysis process have great influence on the recovery rate of sulfuric acid and the retention rate of metal salt, and the stability of the equipment is difficult to control.
4. The diffusion dialysis membrane has small treatment capacity and low separation efficiency, so that diffusion dialysis equipment is huge and investment cost is high. The dialysis membrane replacement costs are also high.
5. Although part of acid can be recovered after the treatment of the diffusion dialysis membrane and recycled for production, the concentration of the recovered acid is limited by the equilibrium concentration, and the concentration of the effective acid is lower than that of the raw material acid, so that the overall recycling rate is not high.
6. Residual liquid generated by recycling sulfuric acid through a diffusion dialysis membrane cannot be directly discharged, a large amount of alkali is consumed in the treatment process, a large amount of A l (OH) 3 and CaSO 4 waste residues are generated, the treatment cost is high, and the waste of aluminum sulfate resources is caused.
Disclosure of utility model
The utility model aims to provide a low-temperature normal-pressure evaporation crystallization recovery device for waste sulfuric acid of electronic aluminum foil, which solves the technical problems.
The aim of the utility model can be achieved by the following technical scheme:
The low-temperature normal-pressure evaporation crystallization recovery device for the electronic aluminum foil waste sulfuric acid comprises an evaporation tower, wherein one side of the lower end of the evaporation tower is sequentially connected with an acid inlet secondary preheater, an acid inlet preheater and an acid inlet pump;
the other side of the lower end of the evaporation tower is sequentially connected with a medium circulating pump, a preheater and a steam heat exchanger, and the steam heat exchanger is connected with the top of the evaporation tower through a connecting pipe to form a circulating loop.
As a further scheme of the utility model: the evaporator is characterized in that a demister, a water distribution system and a filler are sequentially arranged in the evaporator from top to bottom.
As a further scheme of the utility model: the lower part of the evaporation tower is connected with a centrifugal fan through a pipeline, and the centrifugal fan blows cold dry air into the evaporation tower.
As a further scheme of the utility model: and a condensate drain pipe is arranged behind the acid-feeding secondary preheater and is used for automatically flowing the steam condensate cooled by the two heat exchange of the steam heat exchanger and the acid-feeding secondary preheater to the condensate trench for discharging.
As a further scheme of the utility model: the bottom of the evaporation tower is connected with a concentrated acid pump through a pipeline, the concentrated acid pump is connected with a freezing crystallization kettle through a pipeline, and the freezing crystallization kettle is connected with a refrigerator through a pipeline.
As a further scheme of the utility model: the freezing crystallization kettle is connected with a scraper discharging centrifugal machine through a pipeline, the scraper discharging centrifugal machine is connected with a mother liquor tank through a pipeline, and the mother liquor tank is connected with a recovery acid pump through a pipeline.
As a further scheme of the utility model: the acid inlet preheater is connected with the condensate cooler through a pipeline, the condensate cooler is connected with the upper part of the condensing tower through a pipeline, the bottom of the condensing tower is connected with the condensate circulating pump through a pipeline, and the condensate circulating pump is also connected with the preheater through a pipeline;
and a circulation loop is formed among the condensing tower, the condensate circulating pump, the preheater, the acid inlet preheater and the condensate cooler.
As a further scheme of the utility model: the interior of the condensing tower is provided with a foam remover I, a water distribution system and a filler I in sequence from top to bottom.
As a further scheme of the utility model: the condensing tower and the evaporating tower are connected through a pipeline.
As a further scheme of the utility model: the bottom of the condensing tower is connected with a condensate pump through a pipeline.
The utility model has the beneficial effects that:
1. The utility model uses AFC normal pressure evaporation-freezing crystallization method to carry out evaporation crystallization recovery to the waste sulfuric acid of the electronic aluminum foil. The device consists of two independent units of an AFC evaporation system and a freeze crystallization system, and forms a complete evaporation crystallization recovery process.
2. The utility model relates to a low-temperature normal-pressure evaporation crystallization recovery device for waste sulfuric acid of electronic aluminum foil, which is characterized in that waste sulfuric acid (the H2SO4 content is about 15% -30%) is evaporated and concentrated by AFC equipment to form concentrated acid (the H2SO4 is more than or equal to 45%), and then the concentrated acid is subjected to crystallization separation by a freezing crystallization system to obtain recovered sulfuric acid with the sulfuric acid concentration of more than 50%, and aluminum sulfate octadecanoate crystal which can be used as a production raw material of a water purifying agent (polyaluminium sulfate).
3. The phase-change interface of the separation equipment adopts beta-modified high-hardness polypropylene (beta-PPH) nonmetallic materials instead of graphite materials which are resistant to high-concentration sulfuric acid and hydrochloric acid due to low operating temperature, and the phase-change interface has no heat transfer requirement, so that the phase-change interface of the separation equipment has higher corrosion resistance, better economy and longer service life.
4. The utility model fully utilizes the heat energy in the system evaporation, recovers the heat energy of the secondary steam of the system in the form of high-temperature condensate by utilizing washing absorption, and feeds back the heat energy to the temperature rise of the concentrated circulating liquid, so that the temperature of the waste acid is raised by 25-30 ℃, and the energy consumption of steam heat compensation is greatly saved.
5. The utility model fully utilizes the heat energy in the system, utilizes the redundant heat of the condensation circulating liquid to carry out primary preheating and heating on the acid, so that the temperature of the waste acid is increased by 20-30 ℃, and then utilizes the high-temperature sensible heat of the steam condensate to carry out secondary heating on the acid, so that the temperature of the waste acid is further increased by 5-15 ℃, thereby achieving the effect of energy conservation.
6. The working pressure of the AFC of the electronic aluminum foil waste sulfuric acid low-temperature normal-pressure evaporation recovery device is 0-3 kPa, the evaporation temperature is 70-95 ℃, and compared with the traditional negative pressure evaporation device, the electronic aluminum foil waste sulfuric acid low-temperature normal-pressure evaporation recovery device has higher safety and corrosion resistance.
7. The utility model creatively uses the graphite plate heat exchanger impregnated with phenolic resin as heat transfer equipment, so that the AFC of the low-temperature normal-pressure evaporation concentration equipment has higher heat exchange performance (the K value of the heat exchanger is 3-8 times of that of the tube-array and block-hole type graphite heat exchanger), the energy-saving performance of the AFC evaporation technology is greatly exerted, the installation is simple, the occupied area is saved, and the operation and the maintenance are convenient. The acid inlet preheater, the acid inlet secondary preheater, the steam heater and the cooler are all graphite plate type heat exchangers.
8. The utility model creatively uses the graphite plate heat exchanger impregnated by the phenolic resin to recycle the heat in the system through various arrangement modes. When the daily throughput is less than 350 tons, adopting a mode of connecting the multistage heat exchangers in series; when the daily throughput is 350-800 tons, adopting a mode of connecting a plurality of groups of parallel connection and cascade connection; when the daily throughput is more than 800 tons, adopting a heat recovery mode of multiple sets of parallel connection, multiple sets of parallel connection and cascade connection.
9. The low-temperature normal-pressure evaporation crystallization recovery device for the electronic aluminum foil waste sulfuric acid can recover sulfuric acid with concentration of 50% -60%, wherein the equivalent concentration of aluminum ions is less than 0.1N, and the overall recovery rate of sulfuric acid is more than 95%.
10. The advantage of treating the waste sulfuric acid by the electronic aluminum foil corrosion waste acid low-temperature normal-pressure evaporation recovery device is obvious, the expected effect of concentration can be quickly and effectively achieved, the material characteristics are not changed, the concentrated product is stable and reliable, and the acid concentration stably meets the requirement of production and reuse.
Drawings
The utility model is further described below with reference to the accompanying drawings.
Fig. 1 is a schematic view of the overall structure of the present utility model.
In the figure: 1. an acid feeding pump; 2. an acid inlet preheater; 3. feeding acid into a secondary preheater; 4. an evaporation tower; 5. a medium circulation pump; 6. a preheater; 7. a steam heat exchanger; 8. a water distribution system; 9. a filler; 10. a centrifugal fan; 11. a demister; 12. a condensing tower; 13. a freezer; 14. freezing and crystallizing the kettle; 15. concentrating the acid pump; 16. discharging centrifugal machine under scraper; 17. a mother liquor tank; 18. recovering an acid pump; 19. a condensate circulating pump; 20. a condensate cooler; 21. and a condensate pump.
Detailed Description
The following description of the embodiments of the present utility model will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present utility model, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the utility model without making any inventive effort, are intended to be within the scope of the utility model.
Referring to fig. 1, the utility model discloses an electronic aluminum foil waste sulfuric acid low-temperature normal-pressure evaporation crystallization recovery device, which comprises an evaporation tower 4, wherein one side of the lower end of the evaporation tower 4 is sequentially connected with an acid inlet secondary preheater 3, an acid inlet preheater 2 and an acid inlet pump 1; the acid inlet secondary preheater 3 is connected with the acid inlet preheater 2 through a pipeline, and the acid inlet preheater 2 is connected with the acid inlet pump 1 through a pipeline.
The other side of the lower end of the evaporation tower 4 is sequentially connected with a medium circulating pump 5, a preheater 6 and a steam heat exchanger 7, the medium circulating pump 5, the preheater 6 and the steam heat exchanger 7 are connected through pipelines, and the steam heat exchanger 7 is connected with the top of the evaporation tower 4 through a connecting pipe to form a circulating loop. The evaporator tower 4 is internally provided with a foam remover 11, a water distribution system 8 and a filler 9 from top to bottom in sequence.
And a condensate drain pipe is arranged behind the acid-feeding secondary preheater 3 and is used for automatically flowing the steam condensate cooled by the heat exchange of the steam heat exchanger 7 and the acid-feeding secondary preheater 3 to the condensate trench for discharging.
The waste sulfuric acid of the electronic aluminum foil is pumped into a liquid inlet pipeline through an acid inlet pump 1, subjected to heat exchange and temperature rise through an acid inlet preheater 2 and condensate liquid, so that the temperature of the acid inlet is raised to 45-50 ℃, subjected to heat exchange and temperature rise through an acid inlet secondary preheater 3 and steam condensate water to 55-60 ℃, and then enters an evaporation tower 4, and the steam condensate water subjected to heat exchange and temperature reduction automatically flows to a condensate water trench to be discharged. The evaporation tower 4 utilizes a medium circulating pump 5 to pump waste acid at the bottom of the tower into a preheater 6, exchanges heat with high-temperature condensate liquid to raise the temperature to 65-80 ℃, then enters a steam heater 7, raises the temperature of waste acid to 80-100 ℃, enters the evaporation tower 4 through a connecting pipe at the top of the tower, utilizes a water distribution system 8 to uniformly disperse the waste acid on the surface of a filler 9 in the evaporation tower 4, and the filler 9 is an organic composite material and performs heat and mass transfer with dry hot air from bottom to top to form circulation evaporation.
The lower part of the evaporation tower 4 is connected with a centrifugal fan 10 through a pipeline, and the centrifugal fan 10 blows cold dry air into the evaporation tower 4.
The process utilizes a centrifugal fan 10 to blow cold dry air into the lower part of an evaporation tower 4, the air naturally rises, flows through the gap and the surface of a filler 9, fully contacts with the pumped height Wen Feisuan at the top of the tower, carries out heat and mass transfer on the surface of the special filler 9, and partial moisture is vaporized into the air to gradually form high-temperature saturated wet air (85-95 ℃), after small liquid drops are trapped by a foam remover 11, the high-temperature saturated wet hot air formed at the top of the evaporation tower enters a subsequent condensation tower 12, and the evaporation of the moisture in waste acid is reduced until the waste acid reaches the target concentration.
The bottom of the evaporation tower 4 is connected with a concentrated acid pump 15 through a pipeline, the concentrated acid pump 15 is connected with a freezing crystallization kettle 14 through a pipeline, and the freezing crystallization kettle 14 is connected with a freezer 13 through a pipeline. The freezing crystallization kettle 14 is connected with a scraper discharging centrifugal machine 16 through a pipeline, the scraper discharging centrifugal machine 16 is connected with a mother liquor tank 17 through a pipeline, and the mother liquor tank 17 is connected with a recovery acid pump 18 through a pipeline.
Adding the freezing solution mixed by tap water and glycol into a water tank of a refrigerator 13 for cooling to form a designated freezing temperature, and then conveying the designated freezing temperature into a jacket of a freezing crystallizer 14. The concentrated acid is sent to a freezing and crystallizing kettle 14 through a concentrated acid pump 15, and the freezing and crystallizing are carried out under the stirring of a crystallizer stirrer, so that the aluminum sulfate octadeca hydrate slowly forms crystals and grows up. After the freezing crystallization is finished, the crystal slurry flows into a scraper discharging centrifugal machine 16 for solid-liquid separation, the separated aluminum sulfate octadecanoate crystal salt can be sold out or used as a water purifying agent (polyaluminum sulfate) production raw material, the centrifugal mother liquor sulfuric acid flows into a mother liquor tank 17, and the mother liquor sulfuric acid is sent to a production acid preparing unit for recycling through a recycling acid pump 18.
The acid inlet preheater 2 is connected with a condensate cooler 20 through a pipeline, the condensate cooler 20 is connected with the upper part of a condensing tower 12 through a pipeline, the bottom of the condensing tower 12 is connected with a condensate circulating pump 19 through a pipeline, and the condensate circulating pump 19 is also connected with the preheater 6 through a pipeline;
A circulation loop is formed among the condensing tower 12, the condensate circulating pump 19, the preheater 6, the acid inlet preheater 2 and the condensate cooler 20. The interior of the condensation tower 12 is provided with a foam remover I, a water distribution system and a filler I in sequence from top to bottom. The condensing tower 12 and the evaporating tower 4 are connected through a pipeline. The bottom of the condensing tower 12 is connected with a condensate pump 21 through a pipeline.
The condensate circulating pump 19 sends high-temperature condensate at the bottom of the condensing tower to the preheater 6, and the heat of the high-temperature condensate is transferred to the medium side for preheating, so that the raw steam consumption for heating the medium side is saved. The condensate after heat exchange and cooling by the preheater 6 enters the acid-feeding secondary preheater 3, heat is transferred to acid to preheat the acid-feeding secondary preheater, the circulating condensate after secondary cooling enters the condensate cooler 20, the cooled circulating water is utilized to cool to 30-35 ℃, and then the condensate is sent to the top water distribution system of the condensing tower 12 to cool and wash the hot humid air, so that the water vapor carried by the hot humid air is reduced, and the latent heat of the hot humid air is recovered until the high-temperature condensate at the bottom of the condensing tower 12 is formed. The liquid level of the condensing tower 12 is increased by the increasing evaporation condensate, and the condensate is discharged to a workshop for recycling when the liquid level reaches the discharge liquid level by utilizing a condensate pump 21.
The air after cooling and washing contains a trace amount of hydrogen chloride gas, and is discharged to an air inlet pipeline of a unified tail gas washing tower in a factory, and alkali liquor is sprayed and washed and then discharged after reaching standards.
The working principle of the utility model is as follows: aiming at the characteristics of the waste sulfuric acid corroded by the electronic aluminum foil, and combining the process requirements of the acid for production, the evaporative crystallization recovery is considered to be an effective treatment mode for treating the aluminum foil waste acid. The utility model adopts aerodynamic concentration technology (Air Force Concentration, abbreviated as AFC, the same applies below), utilizes the surface gasification evaporation mechanism, and utilizes the full contact of cold dry air blown in from the bottom of an evaporation tower 4 and high Wen Feisuan pumped in from the top of the tower under normal pressure to transfer moisture from waste acid drops and the surface of a liquid film to gas phase, and gradually forms high-temperature saturated humid air (85-95 ℃), thereby realizing the evaporation concentration of waste acid.
The evaporation of water reduces the water temperature in the evaporation tower 4, the system absorbs the latent heat of secondary steam in high-temperature saturated wet air to form high-temperature condensed water, the circulating liquid in the evaporation section is preheated, and saturated raw steam is utilized to secondarily heat the circulating liquid to a set temperature and then enters the evaporation tower for spraying, so that the circulating evaporation is formed. The high-temperature saturated hot and humid air formed at the top of the evaporation tower 4 enters the subsequent condensation tower 12, the hot and humid air is fully contacted with condensed water with lower temperature for heat exchange by utilizing the principle of spray cooling, and the moisture and latent heat carried in the hot and humid air are gradually transferred to a liquid phase while the temperature of the hot and humid air is reduced, so that the recovery of the condensed water and the evaporation heat is realized.
Concentrating the waste sulfuric acid of the electronic aluminum foil by using AFC to form concentrated acid, then entering a freezing crystallization kettle 14 for freezing crystallization to form high-concentration crystal slurry, and obtaining aluminum sulfate octadecanoate crystal salt after centrifugal separation. The content of aluminum in the centrifuged high-concentration sulfuric acid filtrate is greatly reduced, and the high-concentration sulfuric acid filtrate can be recycled to production, so that the recycling utilization of waste acid is realized. The condensate from the AFC evaporation is drained to a condensate tank and can be returned to the workshop for fresh acid dosing and flushing water.
The foregoing describes one embodiment of the present utility model in detail, but the description is only a preferred embodiment of the present utility model and should not be construed as limiting the scope of the utility model. All equivalent changes and modifications within the scope of the present utility model are intended to be covered by the present utility model.
Claims (10)
1. The low-temperature normal-pressure evaporation crystallization recovery device for the electronic aluminum foil waste sulfuric acid is characterized by comprising an evaporation tower (4), wherein one side of the lower end of the evaporation tower (4) is sequentially connected with an acid inlet secondary preheater (3), an acid inlet preheater (2) and an acid inlet pump (1);
The other side of the lower end of the evaporation tower (4) is sequentially connected with a medium circulating pump (5), a preheater (6) and a steam heat exchanger (7), and the steam heat exchanger (7) is connected with the top of the evaporation tower (4) through a connecting pipe to form a circulating loop.
2. The device for recycling the waste sulfuric acid of the electronic aluminum foil through low-temperature normal-pressure evaporation crystallization according to claim 1, wherein a demister (11), a water distribution system (8) and a filler (9) are sequentially arranged in the evaporation tower (4) from top to bottom.
3. The device for recycling the low-temperature normal-pressure evaporative crystallization of the electronic aluminum foil waste sulfuric acid according to claim 1, wherein the lower part of the evaporation tower (4) is connected with a centrifugal fan (10) through a pipeline, and the centrifugal fan (10) blows cold dry air into the evaporation tower (4).
4. The device for recycling the low-temperature normal-pressure evaporative crystallization of the waste sulfuric acid of the electronic aluminum foil according to claim 1, wherein a condensate drain pipe is arranged behind the secondary acid-feeding preheater (3) and is used for automatically flowing steam condensate water cooled by heat exchange between the steam heat exchanger (7) and the secondary acid-feeding preheater (3) to the outside of a condensate water trench.
5. The device for recycling the waste sulfuric acid of the electronic aluminum foil through low-temperature normal-pressure evaporation crystallization according to claim 1, wherein the bottom of the evaporation tower (4) is connected with a concentrated acid pump (15) through a pipeline, the concentrated acid pump (15) is connected with a freezing crystallization kettle (14) through a pipeline, and the freezing crystallization kettle (14) is connected with a freezer (13) through a pipeline.
6. The device for recycling the waste sulfuric acid of the electronic aluminum foil through low-temperature normal-pressure evaporation crystallization according to claim 5, wherein the freezing crystallization kettle (14) is connected with a scraper discharging centrifugal machine (16) through a pipeline, the scraper discharging centrifugal machine (16) is connected with a mother liquor tank (17) through a pipeline, and the mother liquor tank (17) is connected with a recycling acid pump (18) through a pipeline.
7. The device for recycling the low-temperature normal-pressure evaporation crystallization of the waste sulfuric acid of the electronic aluminum foil according to claim 1, wherein the acid inlet preheater (2) is connected with a condensate cooler (20) through a pipeline, the condensate cooler (20) is connected with the upper part of a condensation tower (12) through a pipeline, the bottom of the condensation tower (12) is connected with a condensate circulating pump (19) through a pipeline, and the condensate circulating pump (19) is also connected with a preheater (6) through a pipeline;
And a circulation loop is formed among the condensing tower (12), the condensate circulating pump (19), the preheater (6), the acid inlet preheater (2) and the condensate cooler (20).
8. The device for recycling the waste sulfuric acid of the electronic aluminum foil through low-temperature normal-pressure evaporation crystallization according to claim 7, wherein a demister I, a water distribution system I and a filler I are sequentially arranged in the condensation tower (12) from top to bottom.
9. The device for recycling the low-temperature normal-pressure evaporative crystallization of the waste sulfuric acid of the electronic aluminum foil according to claim 7, wherein the condensing tower (12) and the evaporating tower (4) are connected through a pipeline.
10. The device for recycling the waste sulfuric acid of the electronic aluminum foil through the low-temperature normal-pressure evaporation crystallization according to claim 7, wherein the bottom of the condensing tower (12) is connected with a condensate pump (21) through a pipeline.
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| CN202323606867.5U CN221579727U (en) | 2023-12-28 | 2023-12-28 | Electronic aluminum foil waste sulfuric acid low-temperature normal-pressure evaporation crystallization recovery device |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202323606867.5U CN221579727U (en) | 2023-12-28 | 2023-12-28 | Electronic aluminum foil waste sulfuric acid low-temperature normal-pressure evaporation crystallization recovery device |
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| CN221579727U true CN221579727U (en) | 2024-08-23 |
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| CN202323606867.5U Active CN221579727U (en) | 2023-12-28 | 2023-12-28 | Electronic aluminum foil waste sulfuric acid low-temperature normal-pressure evaporation crystallization recovery device |
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