CN211112234U - Acid recovery device for reverse ion exchange - Google Patents
Acid recovery device for reverse ion exchange Download PDFInfo
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- CN211112234U CN211112234U CN201921461051.9U CN201921461051U CN211112234U CN 211112234 U CN211112234 U CN 211112234U CN 201921461051 U CN201921461051 U CN 201921461051U CN 211112234 U CN211112234 U CN 211112234U
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- Treatment Of Water By Ion Exchange (AREA)
Abstract
The utility model discloses a reverse ion exchange's sour recovery unit, including descaling bath, heat exchanger, filter, ion exchange column, clean water jar and waste water station, the ion exchange column is hollow cylinder structure, the ratio of the height dimension of ion exchange column and internal diameter size is 3:1, the ion exchange column intussuseption is filled with exchange resin granule, the bottom position of ion exchange column is equipped with the acid pickle import, the top position is equipped with the clear water export, the bottom position of filter is equipped with the acid pickle import, the top position is equipped with the clear water export, the descaling bath is connected with acid pickle import pipeline; the lower right valve of the ion exchange column is used for recycling acid and returning to the production line; the upper right valve of the ion exchange column is used for recovering and hanging the metal-containing waste liquid to a waste water station. The utility model simplifies the recycling process of the waste acid liquor, thereby improving the efficiency of the production line; and the pollution can be reduced, and the resource can be recycled, so that the waste of acid resources is reduced, and the equipment and the operating cost are saved.
Description
Technical Field
The utility model relates to an acid recovery device, concretely relates to reverse ion exchange's acid recovery device.
Background
The iron and steel component blank is generally subjected to acid cleaning before surface electroplating and spraying to remove surface oxides, so that the acid cleaning waste liquid and the acid cleaning waste water are generated, wherein the acid cleaning waste liquid has high acid concentration and can recover regenerated acid, a large amount of flushing water, namely the acid cleaning waste water has low acid content and is not economical for recovery, the flushing water is discharged as waste water, different components or different processing requirements have different types and concentrations of used acid, for example, the cleaning of steel workpieces or blanks is generally carried out by using sulfuric acid with the concentration of 250 g/L and is heated to 70 ℃ for cleaning, the waste liquid contains 100-150 g/L of sulfuric acid, 200-250 g/L of ferrous sulfate, the waste water also contains oxidized iron, oil mist, the hydrochloric acid cleaning waste liquid generally contains 280-150 g/L of FeCl, 10-50 g/L of waste acid, the waste water contains 100-150 g/L of sulfuric acid, 200-250 g/L of ferrous sulfate, the waste water, the oxidized iron oxide water, the acid mist, the water, the acid mist and the water, the soil, the water, the.
In the treatment and comprehensive utilization of pickling waste water, the traditional waste acid recovery method comprises the following steps: neutralization, ferric sulfate, evaporation concentration-cooling crystallization, acid regulation-freezing crystallization, alkali liquor-ferrous sulfate coprecipitation, diffusion dialysis-diaphragm electrolysis and the like.
(1) Neutralization process
In the early stage, acid and alkali wastewater is generally treated by a chemical neutralization method, and the specific methods comprise acid and alkali wastewater neutralization, dosing neutralization, filtering neutralization and the like, wherein the filtering neutralization method is generally suitable for acid wastewater with less oil and salt and low acid concentration (less than 2 g/L of sulfuric acid and less than 20-30 g/L of hydrochloric acid and nitric acid), the method is not generally used for treating steel pickling wastewater, the lime neutralization method is most commonly used for treating the steel pickling wastewater, and slaked lime is added into the wastewater to neutralize the wastewater, so that the pH value reaches 5.6-6.5, and the wastewater reaches the national discharge standard and is discharged.
The neutralization method for treating the acidic wastewater is simple and easy, but has the following problems: the management is complicated, the control is not easy, and the wastewater treatment capacity is limited; sulfuric acid, water, FeO, Fe in wastewater3O4And FeSO4Can not be utilized; the gas generated in the treatment process diffuses to cause secondary pollution; the amount of sludge is large and the treatment of the remaining salt residues is difficult. New ways to effectively solve these problems have been sought.
(2) Ferric sulfate process
The method is characterized in that iron in the waste liquid can be recycled, so that the method is emphasized by researchers, and a mature practical technology is gradually formed. The following methods are put into production practice.
The concentration-filtration-natural crystallization method, also known as iron filings method, is characterized by that firstly, the waste liquor of sulfuric acid and iron filings are placed in a reaction tank, fully reacted, then the solution is heated to 100 deg.C, reacted for 2 hr, then heated and concentrated, naturally cooled to make ferrous sulfate crystallize and separate out, finally dewatered and dried by means of drying machine.
The process flow of the concentration filtration natural crystallization method is that the method can recover low, medium and high grade ferrous sulfate from pickling waste water for industrial, agricultural, pharmaceutical and chemical reagents, has the advantages of simple and easy operation, low investment, low cost and the like, but only can recover the ferrous sulfate, but can not recover the sulfuric acid, has small processing capacity, poor product quality and long production period, is relatively suitable for small-scale production of village and town enterprises, and is used for treating the steel rolling pickling waste liquid by a first steel special steel company, and after centrifugal drying, the acid concentration of the residual liquid is 0.5 percent, and the ferrous sulfate is 150-170 g/L.
The main principle of the immersion combustion high-temperature crystallization method is that coal gas and air are combusted to generate high-temperature flue gas, and the high-temperature flue gas is directly sprayed into waste acid water to evaporate water, concentrate sulfuric acid and simultaneously separate out ferrous sulfate.
The technological process of the submerged combustion high-temperature crystallization method comprises the following steps: in the sixty-seven decades of the twentieth century, the waste acid with the concentration of 12-15 percent is improved to 45-57 percent by adopting an immersion combustion high-temperature crystallization method in Shanghai, Tianjin, Jilin and the like, and simultaneously, ferrous sulfate (FeSO) containing one crystal water is produced4.H2O). The method has the advantages of high thermal efficiency, high concentration of the regenerated acid and easy solution of equipment; the defects are that the acid mist is large, combustible gas is needed, and the method is more suitable for treating waste acid with large treatment capacity.
The steam jet vacuum crystallization method sprays the waste acid liquor onto burning flame by using a spray head with high atomization efficiency to evaporate water, so that about 35% of sulfuric acid and part of FeSO can be obtained4.H2And O. The working principle is that the evaporator and the crystallizer are kept in a certain vacuum degree through a steam ejector and a condenser. When the waste liquid passes through the heat-insulating device, the water in the waste liquid is evaporated under the heat-insulating condition, so that the waste liquid is concentrated, the temperature of the waste liquid is reduced, the solubility of ferrous sulfate is correspondingly reduced, and the supersaturation degree of the ferrous sulfate is increased. Meanwhile, the supersaturation degree of the ferrous sulfate is further improved in the evaporator due to the addition of the sulfuric acid. In this case, ferrous sulfate is crystallized. The method requires the used material to have higher corrosion resistance, and is easy to generate secondary pollution or unstable in operation so as not to be normally produced.
(3) Evaporative concentration-cooling crystallization method
The basic principle is that the waste liquid is evaporated and concentrated by negative pressure, and then ferrous sulfate crystals are separated out from the waste liquid at low temperature to obtain regenerated sulfuric acid. Is suitable for recovering ferrous sulfate and sulfuric acid in the pickling waste liquid of large-scale steel plants.
The technological process of evaporation, concentration, cooling and crystallization method comprises the following steps: in the early 70 s of the twentieth century, a process of evaporative concentration, cooling crystallization and hydrochloric acid separation was developed. The whole process does not produce secondary pollution, meets the requirement of harmless treatment and has good economic benefit and environmental benefit.
(4) Acid regulating-freezing crystallization method
The process for treating the waste sulfuric acid pickling liquid by freezing crystallization is to separate the ferrous sulfate crystal by controlling the condition of ferrous sulfate crystallization from the waste liquid. The effects of purifying the pickling waste liquid and recovering ferrous sulfate are achieved. The main process is to add concentrated sulfuric acid into the waste acid washing liquor to adjust the weight percentage concentration of sulfuric acid to 22-25%, then to reduce the temperature of the waste liquid from 20-40 ℃ to 0-3 ℃ by a refrigeration method to reduce the solubility of ferrous sulfate and crystallize and separate out, and then to filter and separate the solid and the liquid. Recovering ferrous sulfate and reusing the regenerated acid without ferrous sulfate.
(5) Coprecipitation method of alkali liquor and ferrous sulfate
The method combines a neutralization method and a ferrous sulfate method to treat the acidic wastewater. The basic principle is that alkali liquor or lime is added into the waste water to neutralize the acid waste water and generate sodium sulfate. The generated sodium sulfate still has certain solubility, and a polyacrylamide flocculant needs to be added to aggregate and settle the metal ions. Two-stage treatment is adopted, the sediment obtained from the first-stage treatment is stirred by a stirrer to destroy the balance between the sediment and ions in a liquid phase, then the sediment is fully reacted by a neutralization tower, and then the second-stage sedimentation treatment is carried out to obtain better effect. The method is suitable for treating the acid wastewater with higher sulfur concentration. Ningbo and Sen steel pipe Limited built in 1995 simultaneously builds an acid wastewater treatment device, the wastewater treatment capacity reaches 10t/h, the floor area is about 300m2, and the total investment is 17 ten thousand yuan.
(6) Diffusion dialysis-diaphragm electrolysis
In the seventies of the twentieth century, the acid washing wastewater is comprehensively treated by using a diffusion dialysis-diaphragm electrolysis method. Waste acid enters a diffusion dialyzer, wherein 204 anion exchange membranes S-203 are arranged in the dialyzer, the two sides of the membranes are respectively a water phase and a waste acid phase, and free acid in the waste acid continuously enters the water phase to become sulfuric acid to be recovered due to the concentration difference of acid existing in the two phases and the selective permeability and the molecular sieve action of the ion exchange membranes. The residual liquid enters a diaphragm electrolytic cell, a cathode and an anode are inserted, an anion exchange membrane F-201 is arranged between the cathode and the anode to form an cathode chamber and an anode chamber, iron ions and sulfate ions in the residual liquid are reduced into pure iron under the action of a direct current electric field by utilizing the selective permeability of the cathode membrane, and the sulfate ions and hydrogen ions are combined into sulfuric acid in the anode chamber. The method has the advantages of simple equipment and high recovery efficiency, and can recover waste acid and extract iron. The disadvantage is the higher power consumption.
An environment-friendly and energy-saving waste acid recovery method (namely acid retardation technology) is newly researched in recent years, but the effect is not good.
The regeneration and utilization of the waste hydrochloric acid are realized by utilizing the function that certain ion exchange resins can absorb acid from waste acid solution and remove metal salt. The waste hydrochloric acid from the waste acid tank enters a clean ferrous salt-containing tank after being filtered by a filtering device, the clean ferrous salt-containing acid flows through a resin bed from the bottom through a pipeline, HCl is absorbed by the resin, and liquid containing other ions is discharged and enters a metal salt recovery system. Thereby achieving acid salt separation. The method has the advantages of short process flow and easy operation; the energy consumption is low; normal temperature treatment can prolong the service life of equipment and pipelines and reduce the escape of chloride. However, the concentration of the hydrochloric acid recovered during the treatment under normal pressure is low, and the hydrochloric acid needs to be added for use.
According to patent No. CN205999182U, the short bed ion exchange resin method needs to separate acid and metal ions under high pressure environment, and the resin is easy to damage and lose efficacy under high pressure for a long time; the operation cost is high, and the separation effect is poor due to the short resin bed.
The existing methods for treating inorganic waste acid have the following disadvantages: although the short bed ion exchange resin method has short process flow, easy operation and low energy consumption, the concentration of the recovered inorganic acid is low during normal temperature treatment, and the inorganic acid can be used only by adding high-concentration acid; the roasting method does not produce new pollutants, and the recovered product can be recycled, but has great pollution to the environment, and the gas containing pollution is a big problem; although the equipment used in the concentration method is easy to scale and difficult to clean, the acid treated by the method can reach high concentration and can be directly utilized; the neutralization method ensures the pH value of the treated substance; the extraction method can separate organic matters from waste acid under certain conditions, but the treated waste acid still contains a large amount of organic matters, so that the treatment is difficult. Therefore, when waste acid is treated, different treatment methods are selected according to specific situations.
Disclosure of Invention
The to-be-solved technical problem of the utility model is to provide reverse ion exchange's sour recovery unit to solve the problem of the recycle of pickle.
For solving the technical problem who exists, the utility model discloses a technical scheme be: the acid recovery device comprises a heat exchanger, an ion exchange column, a clear water tank and a wastewater station, wherein the heat exchanger is respectively provided with a heat energy release inlet, a heat energy release outlet, a heat energy absorption inlet and a heat energy absorption outlet, the heat energy release inlet and the heat energy release outlet are respectively connected with the bottom of a pickling tank and the bottom of the ion exchange column in a production line through pipelines, the heat energy absorption inlet and the heat energy absorption outlet are respectively connected with the bottom of the ion exchange column and the pickling tank in the production line through pipelines, the heat energy of the waste acid liquor is released after the waste acid liquor enters the heat exchanger from the pickling tank in the production line, and then the heat exchanger converts the heat into recovered acid liquor; the ion exchange column is of a hollow cylindrical structure and is filled with ion exchange resin particles; the clean water tank is connected with the top of the ion exchange column through a pipeline, clean water in the clean water tank enters the ion exchange column from the top to desorb acid ions from ion exchange resin, and the acid ions are discharged from the bottom of the ion exchange column, enter the heat exchanger through a heat energy absorption inlet of the heat exchanger to absorb heat, and then are discharged through a heat energy absorption outlet of the heat exchanger to return to a pickling tank in a production line; the waste water station is connected with the top of the ion exchange column through a pipeline, and the waste acid liquid enters the heat exchanger from an acid washing tank in the production line through a heat energy release inlet of the heat exchanger to release heat energy, and is discharged through a heat energy release outlet of the heat exchanger to enter the ion exchange column to adsorb acid ions so as to wash out metal ions in the acid liquid, and the waste water is discharged to the waste water station.
In order to filter solid suspended matter, insoluble solid particles and the like in the spent acid solution, particularly, the acid recovery apparatus of the present invention preferably further comprises a filter installed in a pipe between the pickling tank and the heat exchanger or between the heat exchanger and the ion exchange column.
In order to facilitate collection of the spent acid solution in the pickling tank to improve the use efficiency of the acid recovery device, in particular, the acid recovery device of the present invention preferably further includes a collection tank installed in a pipeline after the heat exchanger.
In order to increase the fluidity of the waste acid liquid and facilitate the control of the acid recovery device, particularly, the acid recovery device preferably further comprises a booster pump, a heat energy release outlet and a clean water tank of the heat exchanger are respectively connected with an inlet of the booster pump through a valve I, a valve II and a pipeline, an outlet pipeline of the booster pump is divided into two pipelines, one pipeline is connected with the top of the ion exchange column through a valve V, and the other pipeline is connected with the bottom of the ion exchange column through a valve VI.
In order to reduce the use amount of clear water, improve the concentration of the recovered acid liquid and facilitate the control of the acid recovery device, particularly, the acid recovery device preferably further comprises an air compressor, and the air compressor and the waste water station are respectively connected with the top of the ion exchange column through a valve III, a valve IV and a pipeline.
In order to facilitate the collection of the purified acid solution in the ion exchange column, so as to improve the use efficiency of the acid recovery device and facilitate the control of the acid recovery device, particularly, the acid recovery device preferably further comprises an acid solution recovery tank and an acid solution recovery pump, wherein the inlet of the acid solution recovery tank is connected with the bottom of the ion exchange column through a valve VIII and a pipeline; the outlet of the acid liquor recovery tank is connected with the heat energy absorption inlet of the heat exchanger after being connected with the acid liquor recovery pump through a pipeline.
In order to facilitate filtering of solid suspended matters, insoluble solid particles and the like in the waste acid liquid and control of the acid recovery device, particularly, a filter is preferably arranged in a pipeline connecting the booster pump and the bottom of the ion exchange column, and a valve VI and a valve VII are respectively arranged on pipelines between the booster pump and the filter and between the filter and the bottom of the ion exchange column.
The ion exchange column 4 may be suitably selected as required, and particularly, the ratio of the height dimension to the inner diameter dimension of the ion exchange column of the present invention is preferably 3: 1.
The invention also discloses a method for recovering acid by reverse ion exchange, which comprises two steps:
the first step is that the waste acid liquid enters an ion exchange column to discharge the metal ions in the washed acid liquid to a waste water station
Firstly, connecting a waste acid solution from a pickling tank, flowing through a heat exchanger, entering an ion exchange column, and discharging the waste acid solution into a pipeline of a waste water station, closing other pipelines, enabling the waste acid solution to enter the heat exchanger from the pickling tank, releasing heat energy, cooling the heat energy, entering the bottom of the ion exchange column, adsorbing acid ions by an exchange resin in the process that the waste acid solution flows from the bottom to the top of the ion exchange column, and finally discharging the waste acid solution from the top of the heat exchanger 2 to the waste water station for metal ion recovery;
the second step is to wash out the acid liquor in the ion exchange column with clean water and arrange the acid liquor to a heat exchanger
The method comprises the following steps of putting clean water in a clean water tank into a pipeline at the top of an ion exchange column, a pipeline from the bottom of the ion exchange column to a heat exchanger and a pipeline from the heat exchanger to a pickling tank, connecting the pipelines, closing other pipelines, desorbing and backwashing acid ions adsorbed on exchange resin in the ion exchange column by using the clean water to obtain purified acid liquor, discharging the purified acid liquor into the heat exchanger from the bottom of the ion exchange column, and returning the acid liquor to the pickling tank in a production line for recycling after absorbing heat energy in the heat exchanger;
and when the second step is completed, returning to the first step to operate again.
In particular, the invention also discloses a specific reverse ion exchange acid recovery method which is divided into three steps,
the first step is that the waste acid liquid enters an ion exchange column to discharge the metal ions in the washed acid liquid to a waste water station
Firstly, opening a valve I, a valve IV, a valve VI and a valve VII, closing other valves, enabling the waste acid liquid to enter a heat exchanger from a pickling tank to release heat energy for cooling, then pressurizing the waste acid liquid discharged from the heat exchanger by using a booster pump, enabling the waste acid liquid to enter a filter for filtering, enabling the waste acid liquid filtered by the filter to enter the bottom of an ion exchange column, enabling the waste acid liquid to be adsorbed by exchange resin in the process of flowing from the bottom to the top of the ion exchange column, and finally, discharging the waste acid liquid from the top of the heat exchanger to a waste water station for metal ion recovery;
the second step is to wash out the acid liquor in the ion exchange column with clean water and arrange the acid liquor to a heat exchanger
Closing the valve I, the valve IV, the valve VI and the valve VII, opening the valve II, the valve V, the valve VIII, the booster pump and the acid liquor recovery pump, adding clear water in the clear water tank into the top of the ion exchange column by using the booster pump, desorbing and backwashing acid ions adsorbed on the exchange resin by the clear water in the process of flowing from the top to the bottom of the ion exchange column to obtain purified acid liquor, discharging the purified acid liquor to the acid liquor recovery tank from the bottom of the ion exchange column, conveying the acid liquor in the acid liquor recovery tank into the heat exchanger by using the acid liquor recovery pump, and returning the acid liquor to a pickling tank in a production line for recycling after absorbing heat energy in the heat exchanger; the third step is that compressed air is utilized to press out the residual acid liquor in the ion exchange column to an acid liquor recovery tank, a valve II and a valve V are closed, a valve III and an air compressor are opened, the compressed air produced by the air compressor enters from the top of the ion exchange column, the compressed air completely discharges the acid liquor in the ion exchange column to the acid liquor recovery tank, the acid liquor in the acid liquor recovery tank is conveyed into a heat exchanger through an acid liquor recovery pump, and the acid liquor returns to an acid washing tank in a production line for recycling after absorbing heat energy in the heat exchanger;
and returning to the first step to operate again after the third step is completed.
In general, the flow rates of the spent acid solution and the clear water and the pressure of the compressed air can be selected as required, and particularly, the spent acid solution in the first step of the acid recovery method of the present invention flows from the bottom to the top of the ion exchange column at a flow rate of 2 to 20 m/h; the clean water in the second step flows from the top to the bottom of the ion exchange column at the flow speed of 2-20 m/h; the compressed air pressure in the third step is maintained at 0.5-3 bar.
The ion exchange column of the present invention should provide sufficient height, and the longer the stacking distance of the ion exchange resin, the better the separation of the acid from the metal is performed. The separation by ion exchange is an important technology of chromatographic separation, and the longer the resin layer is, the farther the liquid flow path is, and the more the separation coefficient is obviously improved.
The invention can evenly feed the waste acid liquid into the reverse ion exchange column, and all the resins can completely contact the waste acid liquid, thereby realizing the function of resin separation in a hundred percent.
The waste acid inlet and outlet of the invention are both provided with heat exchangers, and the heat energy in the waste acid discharged from the production line is converted into the heat energy in the acid return system.
The invention can directly desorb acid ions in the ion exchange resin by using clear water without using other chemical agents.
The invention relates to a reverse ion exchange acid recovery device, which aims to simplify the production flow of a steel industry processing plant so as to improve the efficiency of a production line; and the pollution can be reduced, and the resource can be recycled, so that the waste of acid resources is reduced, and the equipment and the operating cost are saved. Table 1 below shows experimental data of the acid solution after the waste acid solution is purified by the acid recovery device.
Table 1 spent acid liquor recovery experimental data
Advantageous effects
The utility model discloses can get into waste acid liquid on average in the reverse ion exchange column, all resin homoenergetic contact waste acid liquid completely, lead to the hundred resin of utilizing to make the function of separation of percentage, improve the separation effect, reverse ion exchange column does and reduces the energy consumption, does to reduce the loss of resin to the life of extension resin. The waste acid inlet and outlet are both provided with heat exchangers, the heat in the waste acid discharged from the production line can be converted into the heat in the acid return system, the energy consumption is greatly reduced, and the temperature of the waste acid before entering the ion exchange column can be reduced, so that the service life of the resin is prolonged. The acid ions in the ion exchange resin can be directly desorbed by using clear water, so that the whole process becomes more environment-friendly and cleaner, and the acidity is also improved.
Drawings
FIG. 1 is a schematic diagram of an acid recovery unit for reverse ion exchange, wherein: 1-a pickling tank, 2-a heat exchanger, 3-a filter, 4-an ion exchange column, 5-a clean water tank, 6-a wastewater station and 7-a valve;
FIG. 2 shows a structure diagram of a reverse waste acid purification and metal recovery apparatus, wherein the drawing shows the following marks: 1-a pickling tank, 2-a heat exchanger, 3-a filter, 4-an ion exchange column, 5-a clean water tank, 6-a wastewater station, 8-a booster pump, 9-an air compressor, 10-an acid liquor recovery tank, 11-an acid liquor recovery pump, 71-a valve I, 72-a valve II, 73-a valve III, 74-a valve IV, 75-a valve V, 76-a valve VI, 77-a valve VII, and 78-a valve VIII;
FIG. 3 shows the test results of the reverse ion-exchange acid recovery method of the present invention for the waste hydrochloric acid solution of iron and steel smelters;
FIG. 4 shows the test results of the conventional acid recovery method for the waste hydrochloric acid solution in the iron and steel smelting plant;
FIG. 5 shows the test results of the acid recovery method of reverse ion exchange for waste hydrochloric acid solution of hot dip galvanizing plating plant according to the present invention;
description of the drawings: any container suitable for the present invention, such as a tank, a pool, a bucket, etc., is collectively referred to as a tank.
Detailed Description
The present invention is described in further detail below with reference to specific embodiments so that advantages and features of the invention may be more readily understood by those skilled in the art, thereby making more specific definitions of the intended scope of the invention.
As shown in the attached figure 1, the acid recovery device for reverse ion exchange comprises a pickling tank 1, a heat exchanger 2, a filter 3, an ion exchange column 4, a clean water tank 5 and a waste water station 6, wherein the ion exchange column 4 is of a hollow cylindrical structure, the ratio of the height dimension to the inner diameter dimension of the ion exchange column 4 is 3:1, ion exchange resin particles are filled in the ion exchange column 4, a waste acid liquid inlet is formed in the bottom position of the ion exchange column 4, a clean water outlet is formed in the top position of the ion exchange column 4, a waste acid inlet is formed in the bottom position of the filter 3, a clean water outlet is formed in the top position of the filter 3, and the pickling tank 1 is connected with the; the lower right valve 7 of the ion exchange column 4 is used for recovering acid and returning to the production line; the upper right valve 7 of the ion exchange column 4 is used for recovering and hanging the metal-containing waste liquid to the waste water station 6.
The pickle liquor is discharged from pickling tank 1 in the production line, and the heat energy of acidizing fluid can be liberated when entering heat exchanger 2, then heat exchanger 2 can be with heat conversion to retrieve in the acidizing fluid, simultaneously, the acidizing fluid can get into the collecting pit after heat exchanger 2 cools down, and when the acidizing fluid is collected to certain water yield, the acidizing fluid just can advance to go into filter 3 and carry out impurity filtering to ensure that most impurity has been carried out before the acidizing fluid gets into the ion exchange column and gets rid of.
After the acid liquor leaves the filter 3, the acid liquor enters the ion exchange column 4 from the bottom to separate acid ions from metal ions, the wastewater containing the metal ions is separated out and is discharged to the wastewater station 6 to be recycled by metal ions, the acid ions stay in the resin of the ion exchange column 4, and then the clear water enters the ion exchange column 4 from the top to desorb the acid ions from the resin, so that the acid liquor leaves the ion exchange column 4 and can return to a production line for acid washing and reusing.
As shown in fig. 2, a reverse waste acid purification and metal recovery method and apparatus comprises an apparatus made of corrosion-resistant materials: the pickling tank 1, the heat exchanger 2, the filter 3, the ion exchange column 4, the clean water tank 5, the waste water station 6, the booster pump 8, the air compressor 9, the acid liquor recovery tank 10, the acid liquor recovery pump 11 and the valve are electrically connected with an automatic control circuit;
the heat energy release inlet of the heat exchanger 2 is directly connected to the pickling tank 1 of the production line by a water pipe, the liquid inlet of the booster pump 8 is respectively provided with two water pipes, each water pipe is respectively provided with a valve I71 and a valve II 72, the heat energy release outlet of the heat exchanger 2 is provided with a valve I71 which is connected to the inlet of the booster pump 8 by a water pipe, and the clean water tank 5 is provided with a valve II 72 which is also connected to the inlet of the booster pump 8. The outlet of the booster pump 8 is respectively connected to the top of the filter 3 and the top of the ion exchange column 4 by water pipes, and the two water pipes are respectively provided with a valve VI 76 and a valve V75. The outlet of the filter 3 is connected to the bottom of the ion exchange column 4 by a water pipe provided with a valve VII 77. The other water pipe is provided with a valve VIII 78 which is connected to the acid liquor recovery tank 10 from the bottom of the ion exchange column 4. The outlet at the top of the ion exchange column 4 is connected with three pipes, one water pipe is fixedly provided with a valve V75 connected to the outlet of the booster pump 8, the other water pipe is fixedly provided with a valve IV 74 connected to the waste water station 6 by a water pipe, and the third pipe is fixedly provided with a valve III 73 connected with the air compressor 9;
the acid liquor recovery tank 10 is connected to the acid liquor recovery pump 11 by a water pipe, the outlet of the acid liquor recovery pump 11 is connected to the other inlet of the heat exchanger 2 by a water pipe (heat energy absorption), and the outlet of the heat exchanger 2 for heat energy absorption is connected to the pickling tank 1 returned to the production workshop by a water pipe for direct use.
The acid recovery method of reverse ion exchange comprises the following three steps:
the first step is that the waste acid liquid enters an ion exchange column 4 and metal ions in the washed acid liquid are discharged to a waste water station 6
After the pickling tank of the production line is used for a period of time, the metal content of the acid liquor is increased to reduce the pickling efficiency, at the moment, the automatic control circuit is used for controlling the opening of the valve I71, the valve IV 74, the valve VI 76 and the valve VII 77 and the closing of other valves, the acid liquor with the temperature of over 60 ℃ (also serving as the waste acid liquor) enters the heat exchanger 2 from the pickling tank 1 to release heat energy for cooling, then, the automatic control circuit is used for controlling the booster pump 8 to pressurize the waste acid liquor discharged from the heat exchanger 2 to enter the filter 3 for filtering, and therefore solid suspended matters and insoluble solid particles in the waste acid liquor are filtered; the waste acid solution filtered by the filter 3 enters the bottom of the ion exchange column 4, and the waste acid solution absorbs acid ions by the exchange resin in the process of flowing from the bottom to the top of the ion exchange column 4 at the flow rate of 2-20m/h, so that the resin in the ion exchange column 4 can effectively and averagely contact the waste acid solution; the waste acid is subjected to extremely fine color separation, most heavy metal ions (85-95%) in the waste acid are discharged to a waste water station 6 through a valve IV 74 for metal recovery, and most acid ions (85-98%) in the waste acid are adsorbed and stay in an ion exchange column 4.
The second step is to wash out the acid solution in the ion exchange column 4 with clear water and discharge the acid solution to the acid solution recovery tank 10
Closing the valve I71, the valve IV 74, the valve VI 76 and the valve VII 77, opening the valve II 72, the valve V75, the valve VIII 78, the booster pump 8 and the acid liquor recovery pump 11, adding the clear water in the clear water tank 5 into the top of the ion exchange column 4 by using the booster pump 8, desorbing and backwashing acid ions adsorbed on the exchange resin by using the clear water in the process of flowing from the top to the bottom of the ion exchange column 4 at the flow rate of 2-20m/h to obtain purified acid liquor, and purifying the acid liquor after separating the acid liquor from heavy metals, wherein the concentration is correspondingly increased. The purified acid liquor is discharged to an acid liquor recovery tank 10 from the bottom of the ion exchange column 4, the acid liquor in the acid liquor recovery tank 10 is conveyed into a heat exchanger 2 through an acid liquor recovery pump 11, and the acid liquor is returned to an acid washing tank 1 in the production line for recycling after absorbing heat energy in the heat exchanger 2;
the third step is to press out the residual acid solution in the ion exchange column 4 to the acid solution recovery tank 10 by using compressed air
Closing a valve II 72 and a valve V75, opening a valve III 73 and an air compressor 9, allowing compressed air generated by the air compressor 7 to enter from the top of the ion exchange column 4, maintaining the pressure of the compressed air at 0.5-3 bar, completely discharging acid liquor in the ion exchange column 4 to an acid liquor recovery tank 10 by the compressed air, conveying the acid liquor in the acid liquor recovery tank 10 into a heat exchanger 2 through an acid liquor recovery pump 11, and returning the acid liquor to an acid washing tank 1 in a production line for recycling after the heat energy is absorbed by the acid liquor in the heat exchanger 2;
and returning to the first step to operate again after the third step is completed. The automatic control circuit can also set the running times of the equipment device according to the requirements of the production line, thereby achieving the purpose of effectively utilizing resources.
The acid liquor enters the ion exchange column 4 from the bottom of the ion exchange column 4, so that the resin in the ion exchange column 4 can effectively and averagely contact the waste acid liquor; the acid liquor in the waste acid is adsorbed, so that the adsorption area, the adsorption efficiency and the adsorption quantity are improved; the acid liquor enters from the bottom of the ion exchange column 4, so that the internal pressure of the resin bed can be effectively reduced, the damage of the resin can be reduced, and the height and the area of the ion exchange column 4 can be increased by 2: 1-10: 1. Thereby greatly increasing the effect of ion exchange chromatography, purifying the produced acid liquor, and the heavy metal in the purified acid is only 2-10 percent, and the recovery rate of the acid reaches 85-98 percent.
The invention uses the heat exchanger 2, and transfers the heat in the acid liquor from the pickling tank 1 of the production line to the acid liquor returned from the acid liquor recovery tank 10 to the pickling tank 1 of the production line by using the heat exchanger 2, so that the temperature of the waste acid liquor entering the resin bed can be reduced, the loss of the resin is reduced, and the service life of the equipment is prolonged. The compressed air is provided by the compressed air machine 9, the acid liquor in the ion exchange column 4 is completely pressed out of the ion exchange column 4, the use amount of clear water can be greatly reduced, the concentration of the recovered acid liquor is improved, the recovered acid liquor can be directly used when being returned to a production line, and the supplement of new acid liquor is reduced by 85-95%.
Through the mode, the waste acid is adsorbed by the ion exchange column 4, and the purification and collection of acid liquor in the waste liquid and the discharge of metal impurities are realized by opening and closing each valve, so that the aims of reducing the waste acid treatment cost, reducing the energy consumption, reducing the production cost, improving the waste acid recycling rate and promoting the enterprise development are fulfilled.
Example 1:
in the electroplating and metal surface treatment industries, a large amount of acid is used as a cleaning solution and an electrolyte, and when metal ions in the acid reach a certain concentration, the waste acid is replaced by fresh acid liquor to generate a large amount of waste acid. A ー stock sulfuric acid or hydrochloric acid pickling system in the steel industry produces waste acid containing about 50-200g/l of acid and 150-300g/l of iron salt; in the production process of stainless steel, the mixed acid of nitric acid and hydrofluoric acid is used for pickling to remove the oxide layer on the metal surface, and the generated stainless steel pickling waste hydrochloric acid HCl contains about 5-15% of nitric acid HNO32-5% of metal salt of hydrofluoric acid HF 30-60 g/L, separating acid and metal salt from waste acid after the waste acid liquid is subjected to particle filtration by an acid recovery layer analyzer, alternately performing feeding adsorption and elution in opposite directions, circularly and respectively pumping waste acid, clear water and compressed air, returning the purified acid liquid separated from the effluent liquid to production for direct use, and sending the heavy metal-containing wastewater to a wastewater station for recovery.
FIGS. 3 and 4 are the results of tests on the waste hydrochloric acid solution from steel smelting plant by the present apparatus and method, respectively, FIG. 3 shows the use of the reverse waste acid feeding method of the present invention, FIG. 4 shows the use of the conventional acid solution recovery method, the acid resin bed diameter is 150mm and the height is 750mm, the waste acid solution flow rate is 10m/hr, the pressure is 1bar, the acid concentration of the waste acid is 12% and the total iron concentration is 150 g/L. the variation of the acid and iron ion concentrations pumped in and discharged out:
first stage, low acid water stage: the acid ions are absorbed in the ion exchange column 4, the metal iron ions are discharged out of the ion exchange column 4 until the collection is stopped when the concentration of the acid ions in the effluent liquid rises to 0.25 time of the concentration of the metal ions in the waste acid fed, the metal water in the section is discharged to a waste water station for recovering the metal,
the second section, high-salt and medium-acid liquid section, namely the ion exchange column 4 is run with acid ions, when the waste acid liquid continuously enters, the acid ions start to be discharged out of the ion exchange column 4 in a large amount until the acid ions and the iron ions rise to the same concentration as the fed waste acid liquid,
a third stage and a high-acid high-salt solution stage: after the section B is finished, the ion exchange column 4 is in a saturated state until the concentration of the metal ions in the effluent liquid reaches the concentration of the metal ions in the feed waste acid,
the invention has obvious improvement on the efficiency of the ion exchange column 4, and compared with the traditional waste acid recovery process, the invention can increase the utilization rate of resin by 10-30 percent.
Example 2
The hot dip galvanizing electroplating plant performs acid cleaning before electroplating by using hot hydrochloric acid liquid, the concentration of the used acid liquid is 15 percent, the total iron content is 130 g/L, the hot waste acid (the temperature is about 60 ℃ below zero) enters a heat exchanger, the temperature is reduced to 35 ℃, particles are removed by a filter through a booster pump, the hot waste acid reversely enters an acid return resin bed filled with acid-absorbing resin, the resin (strong alkaline ion exchange resin) adsorbs acid, the acid ion concentration in effluent liquid at the top of the resin bed is low, the metal ion concentration is high, the effluent liquid is discharged to a wastewater station for metal recovery, when the concentration of the acid ion in the effluent liquid reaches 0.5 time of the acid liquid, the acid inlet is stopped, clean water is eluted to produce recycled acid, the recycled acid flows in a direction opposite to the flow direction of the waste acid, when the concentration of the acid ion in the effluent liquid of the resin bed is reduced to 0.5 time of the acid liquid, the water inlet is stopped, compressed air is introduced, the residual liquid in the resin bed is.
The acid resin bed diameter was 750mm and height was 3000mm, the spent acid solution (reverse fed into the resin bed) flow rate was 10m/hr, the pressure was 2bar, and the concentration of acid and iron ions pumped in and discharged was varied as shown in FIG. 5.
Section A, low-acid high-salt water section: the acid liquid reversely enters the ion exchange column 4, and H in the effluent liquid+The effluent liquid with low concentration and high heavy metal concentration is discharged to a wastewater station 6 for metal recovery treatment, the collection is stopped until the concentration of acid ions in the effluent liquid is increased to 0.5 time of that in the feed waste acid, and the collection liquid in the section A is recycled as heavy metal.
B section and pure acid section: clear water enters from the top of the ion exchange column 4 until the effluent liquid is H+Stopping collecting when the concentration is reduced to 0.5 time, wherein the collected liquid in the D section is the recovered pure acid.
After the section B is finished, the section C utilizes compressed air to be injected into the ion exchange column 4, and the section is collected to be a pure acid section.
Table 2 shows the change in the acid and iron ion concentration for each stage.
TABLE 2 variation of acid and iron ion concentration in each stage
Injecting: total Fe is Fe2+And Fe3+。
The test realizes the efficiency of the invention on waste acid recovery, and the waste acid recovery rate reaches 92%. Table 3 shows a comparison of the inventive process with conventional APU technology
TABLE 3 comparison of the Process of the present invention with conventional APU technology
While the above description is directed to the preferred embodiment of the waste acid purification and recovery apparatus, it will be understood by those skilled in the art that various changes and modifications may be made without departing from the spirit and scope of the invention.
Claims (8)
1. Reverse ion exchange's acid recovery unit, including heat exchanger (2), ion exchange column (4), clear water jar (5) and waste water station (6), its characterized in that:
the heat exchanger (2) is respectively provided with a heat energy release inlet, a heat energy release outlet, a heat energy absorption inlet and a heat energy absorption outlet, the heat energy release inlet and the heat energy release outlet are respectively connected with the bottoms of the pickling tank (1) and the ion exchange column (4) in the production line through pipelines, the heat energy absorption inlet and the heat energy absorption outlet are respectively connected with the bottom of the ion exchange column (4) and the pickling tank (1) in the production line through pipelines, the heat energy of the waste acid liquor is released after the waste acid liquor enters the heat exchanger (2) from the pickling tank (1) in the production line, and then the heat exchanger (2) converts the heat into recovered acid liquor;
the ion exchange column (4) is of a hollow cylindrical structure, and ion exchange resin particles are filled in the ion exchange column (4);
the clean water tank (5) is connected with the top of the ion exchange column (4) through a pipeline, clean water in the clean water tank (5) enters the ion exchange column (4) from the top to desorb acid ions from ion exchange resin, is discharged from the bottom of the ion exchange column (4), enters the heat exchanger (2) through a heat energy absorption inlet of the heat exchanger (2) to absorb heat, and is discharged through a heat energy absorption outlet of the heat exchanger (2) to return to the pickling tank (1) in the production line;
the waste water station (6) is connected with the top of the ion exchange column (4) through a pipeline, and after the waste acid liquor enters the heat exchanger (2) from the pickling tank (1) in the production line through a heat energy release inlet of the heat exchanger (2) to release heat energy, the waste water is discharged through a heat energy release outlet of the heat exchanger (2) and enters the ion exchange column (4) to adsorb metal ions in the acid liquor to be washed out, and the waste water is discharged to the waste water station (6).
2. The acid recovery device of claim 1, wherein: the acid recovery device also comprises a filter (3), and the filter (3) is arranged in a pipeline between the pickling tank (1) and the heat exchanger (2) or between the heat exchanger (2) and the ion exchange column (4).
3. The acid recovery device of claim 1, wherein: the acid recovery device further comprises a collection tank which is installed in the pipeline after the heat exchanger (2).
4. The acid recovery device of claim 1, wherein: the acid recovery device further comprises a booster pump (8), a heat energy release outlet of the heat exchanger (2) and the clean water tank (5) are respectively connected with an inlet of the booster pump (8) through a valve I (71), a valve II (72) and a pipeline, an outlet pipeline of the booster pump (8) is divided into two pipelines, one pipeline is connected with the top of the ion exchange column (4) through a valve V (75), and the other pipeline is connected with the bottom of the ion exchange column (4) through a valve VI (76).
5. The acid recovery device of claim 1, wherein: the acid recovery device further comprises an air compressor (9), wherein the air compressor (9) and the waste water station (6) are respectively connected with the top of the ion exchange column (4) through a valve III (73), a valve IV (74) and a pipeline.
6. The acid recovery device of claim 1, wherein: the acid recovery device also comprises an acid liquor recovery tank (10) and an acid liquor recovery pump (11), wherein the inlet of the acid liquor recovery tank (10) is connected with the bottom of the ion exchange column (4) through a valve VIII (78) and a pipeline; the outlet of the acid liquor recovery tank (10) is connected with the heat energy absorption inlet of the heat exchanger (2) after being connected with the acid liquor recovery pump (11) through a pipeline.
7. The acid recovery device of claim 4, wherein: install filter (3) in the pipeline that booster pump (8) and ion exchange column (4) bottom are connected, install valve VI (76) and valve VII (77) respectively on the pipeline between booster pump (8) and filter (3) and the bottom of ion exchange column (4).
8. The acid recovery device of claim 1, wherein: the ratio of the height dimension to the inner diameter dimension of the ion exchange column (4) is 3: 1.
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