CN110066080B - Sludge recycling process in aluminum profile processing - Google Patents
Sludge recycling process in aluminum profile processing Download PDFInfo
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- CN110066080B CN110066080B CN201910264918.XA CN201910264918A CN110066080B CN 110066080 B CN110066080 B CN 110066080B CN 201910264918 A CN201910264918 A CN 201910264918A CN 110066080 B CN110066080 B CN 110066080B
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F7/00—Compounds of aluminium
- C01F7/48—Halides, with or without other cations besides aluminium
- C01F7/56—Chlorides
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
- C01G37/00—Compounds of chromium
- C01G37/003—Preparation involving a liquid-liquid extraction, an adsorption or an ion-exchange
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
- C01G37/00—Compounds of chromium
- C01G37/04—Chromium halides
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
- C01G53/00—Compounds of nickel
- C01G53/003—Preparation involving a liquid-liquid extraction, an adsorption or an ion-exchange
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
- C01G53/00—Compounds of nickel
- C01G53/08—Halides
- C01G53/09—Chlorides
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/16—Nature of the water, waste water, sewage or sludge to be treated from metallurgical processes, i.e. from the production, refining or treatment of metals, e.g. galvanic wastes
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Abstract
The invention provides a sludge recycling process in aluminum profile processing, which comprises pulp mixing, extraction and back extraction, wherein the pulp mixing comprises the steps of performing acid leaching and pressure filtration on sludge generated in the aluminum profile processing to obtain filtrate and filter residues; then extracting the filtrate, wherein the extraction can be divided into single-stage extraction and cascade extraction, and a loaded organic phase and a final raffinate are obtained after extraction; and then carrying out back extraction on the loaded organic phase, and leading out an aluminum chloride solution, a nickel chloride solution and a chromium chloride solution at different positions of a back extraction system. The sludge is recycled into chemical products by the sludge recycling process in the aluminum profile processing, metal aluminum in the sludge is converted into an aluminum chloride solution, metal nickel is converted into a nickel chloride solution, metal chromium is converted into a chromium chloride solution, and the recovery rate of aluminum nickel chromium ions in the sludge can reach 99% after cascade extraction and back extraction.
Description
Technical Field
The invention relates to a sludge recycling process in aluminum profile processing, and belongs to the technical field of sludge resource recycling processes.
Background
In the process of processing and producing the aluminum profile, a large amount of colloidal waste liquid is generated when the surface of the aluminum profile is treated, the colloidal waste liquid is commonly called sludge after precipitation treatment, the sludge contains heavy metals such as nickel, chromium and the like, belongs to dangerous waste, and contains a large amount of aluminum elements, the treatment mode of the sludge is generally that enterprises entrust qualified units to carry out treatment, such as landfill or incineration and the like, and the entrust to the outside is high in cost and limited in entrust amount.
At present, most of dangerous wastes generated by aluminum profile enterprises are in a state of piling up to be treated, so that a large amount of land is occupied, and a large amount of aluminum resources are wasted. Therefore, a process technology capable of separating and recycling the sludge in the surface treatment of the aluminum profile containing nickel, chromium and aluminum is developed, the pressure of regional environmental protection is relieved, the resource utilization rate of the aluminum profile industry is improved, and the method has great significance for changing waste into valuable and saving energy and reducing emission.
Disclosure of Invention
In view of the above, the invention provides a sludge recycling process in aluminum profile processing, which specifically adopts P507+ sulfonated kerosene + n-octane + sodium hydroxide as an extractant to extract cations such as aluminum nickel chromium, and the like, in a cascade extraction system, the load extraction of ions is achieved by controlling the flow-to-flow ratio, the organic phase loaded with metal ions is separated from the extracted filtrate, then hydrochloric acid + water is used for carrying out back extraction, the valuable and environmentally harmful metal ions in the loaded organic phase are separated through a back extraction system, and aluminum chloride, nickel chloride and chromium chloride products with the purity of more than 99% are obtained at different positions in process equipment; wherein, the aluminum chloride reaches the national quality standard, and the back extraction wastewater can be discharged after reaching the standard through neutralization, precipitation and filter residue.
The technical means adopted by the invention to achieve the above purpose are as follows.
A sludge recycling process in aluminum profile processing specifically comprises the following steps:
(A) and (3) size mixing, which comprises the steps of putting sludge generated in the aluminum profile processing into a reaction kettle for acid leaching and filter pressing.
Wherein, the acid leaching adopts 31 wt% industrial hydrochloric acid, the hydrochloric acid and the sludge are proportioned according to the volume ratio of 2:1, then the mixture is added into a reaction kettle, water is added after the stirring, and the stirring and the dissolution are continued until the liquid-solid volume ratio is 500; wherein, in the stirring process, metal ions in the sludge are dissolved, and the main reaction equation is as follows:
Ni(OH)2+2HCl＝NiCl2+2H2O
Cr(OH)3+3HCl＝CrCl3+3H2O
Al(OH)3+3HCl＝AlCl3+3H2O
Fe(OH)3+3HCl＝FeCl3+3H2O
Ca(OH)2+2HCl＝CaCl2+2H2O
Mg(OH)2+2HCl＝MgCl2+2H2O
and then carrying out filter pressing on the obtained solid-liquid mixture to obtain filtrate and filter residue.
(B) Extracting, namely preheating the extracting agent and the filtrate obtained in the step (A) in an electric heating reaction kettle respectively, and then introducing the preheated extracting agent and the filtrate into an extraction system respectively for mixing and stirring reaction.
Wherein the volume ratio of the filtrate to the extracting agent is 1: 1.25-1: 1.65, the filtrate enters from a heavy phase feed inlet of the centrifugal extractor, and the extractant enters from a light phase feed inlet of the centrifugal extractor; wherein the extracting agent is prepared by mixing 30 percent of P507, 60 percent of sulfonated kerosene and 10 percent of normal octane by volume fraction and adding sodium hydroxide to reach the saponification rate of 30 to 50 percent; wherein P507 is 2-ethylhexyl phosphate 2-ethylhexyl ester, and the general molecular formula is HA; wherein the extraction reaction equation in the extraction system is as follows:
NiCl2+2(HA)2＝Ni(HA2)2+2HCl
CrCl3+3(HA)2＝Cr(HA2)3+3HCl
AlCl3+3(HA)2＝Al(HA2)3+3HCl
after extraction, a loaded organic phase and a final raffinate are obtained.
(C) And (C) stripping, namely feeding the loaded organic phase obtained in the step (B) into a stripping system, and stripping by using 31 wt% of industrial hydrochloric acid.
Wherein the back-extraction reaction equation in the back-extraction system is as follows:
Al(HA2)3+3HCl＝AlCl3+3(HA)2
Ni(HA2)2+2HCl＝NiCl2+2(HA)2
Cr(HA2)3+3HC＝CrCl3+3(HA)2
and in the first section of centrifugal extractor, 31 wt% of industrial hydrochloric acid and water are added into a heavy phase inlet, the pH value of the mixed phase is controlled to be 2.0-2.5, and the hydrochloric acid reversely extracts aluminum ions loaded in the extractant to obtain an aluminum chloride solution.
And in the second section of centrifugal extractor, 31 wt% of industrial hydrochloric acid and water are added into a heavy phase inlet, the pH value of the mixed phase is controlled to be 2.8-3.5, and the hydrochloric acid reversely extracts nickel ions loaded in the extractant to obtain a nickel chloride solution.
And in the third centrifugal extractor, 31 wt% of industrial hydrochloric acid and water are added into a heavy phase inlet, the pH value of the mixed phase is controlled to be 4.0, and the hydrochloric acid reversely extracts chromium ions loaded in the extracting agent to obtain a chromium chloride solution.
And (3) leading out an aluminum chloride solution, a nickel chloride solution and a chromium chloride solution at the different stages of the back extraction system, and also obtaining back extraction wastewater and a residual organic phase.
In the acid leaching process in the step (A), after hydrochloric acid and sludge are added into a reaction kettle, stirring is needed for 10 minutes, and then water is added for continuous stirring.
The extraction process of the step (B) can adopt single-stage extraction or cascade extraction.
When the step (B) adopts cascade extraction, at least two centrifugal extractors are connected in series to carry out cascade countercurrent extraction.
And (C) allowing the filtrate obtained in the step (A) to enter from a heavy phase inlet of a first-stage centrifugal extractor, allowing the filtrate subjected to the first-stage extraction to flow out from a heavy phase outlet, circulating to a heavy phase inlet of a next-stage centrifugal extractor through a pipeline for repeated extraction, performing repeated extraction through an n-stage centrifugal extractor, and allowing the filtrate to flow out from a heavy phase outlet of a last-stage centrifugal extractor of the extraction system to obtain the final raffinate.
The extractant enters from the light phase inlet of the last stage of centrifugal extractor, flows out from the light phase outlet to the light phase inlet of the last stage of centrifugal extractor, and flows out from the light phase outlet of the first stage of centrifugal extractor of the extraction system after being repeatedly used, so as to obtain a loaded organic phase.
And the flow ratio R of the organic phase flow to the filtrate flow in the cascade extraction process is controlled to be 0.8.
The reaction time of each stage in the cascade extraction process is 5-8 minutes.
The temperature of the filtrate in the extraction system in the step (B) is controlled to be 40-45 ℃, and the temperature of the organic phase is controlled to be 38-42 ℃.
The final raffinate obtained in step (B) may be further pumped to the acid leaching process in step (A) for use.
And (C) directly refluxing the residual organic phase obtained in the step (C) to an extraction system, and reusing the residual organic phase as an extractant.
The reaction time of each stage in the back extraction process of the step (C) is 5-8 minutes.
The invention has the technical effects that: the sludge is recycled into chemical products through the sludge recycling process in the aluminum profile processing, metal aluminum in the sludge is converted into an aluminum chloride solution, metal nickel is converted into a nickel chloride solution, metal chromium is converted into a chromium chloride solution, and the recovery rate of aluminum nickel chromium ions in the sludge can reach 99% after cascade extraction and back extraction. The method realizes the great reduction of sludge and the sustainable utilization of resources in the aluminum profile processing, is beneficial to solving the sludge treatment problem in the aluminum profile industry, reducing the environmental protection pressure of the aluminum profile industry and reducing the environmental pollution on the one hand, and reduces the environmental protection and economic cost of related enterprises on the other hand, thereby filling the technical blank of sludge treatment and resource conversion in the aluminum profile industry in China.
Drawings
FIG. 1: the invention discloses a flow schematic diagram of an embodiment of a sludge recycling process in aluminum profile processing.
Detailed Description
The invention provides a sludge recycling process in aluminum profile processing, and the process adopts sludge containing nickel, chromium, aluminum and other metals as the initial raw material of the process because waste liquid containing nickel, chromium, aluminum and other metals in the aluminum profile processing process is made into mud after the process is produced, and the waste liquid containing the metals to be recycled is conveniently collected and transported after being made into mud. Heavy metal ions in the nickel-chromium-aluminum-containing sludge exist in the form of hydroxide or carbonate, and when the pH value is more than 2, the metal ions are dissolved, so that the dissolution process adopts acid dissolution to dissolve the metal ions. Therefore, before extraction, the sludge needs to be mixed, dissolved and slurried by hydrochloric acid and raffinate wastewater, then is subjected to filter pressing to obtain initial filtrate, and then is introduced into extraction and back extraction process equipment for repeated extraction and recovery.
As shown in fig. 1, the process steps of one embodiment of the sludge recycling process in the aluminum profile processing of the invention are as follows:
(A) slurry mixing, which comprises the steps of putting sludge generated in the aluminum profile processing into a reaction kettle for acid leaching and filter pressing;
wherein, the acid leaching adopts 31 wt% industrial hydrochloric acid, the hydrochloric acid and the sludge are proportioned according to the volume ratio of 2:1, then the mixture is added into a reaction kettle, the mixture is stirred for 10 minutes, then water is added to continue stirring and dissolving, and the liquid-solid volume ratio is controlled to be 500 through the adding weight of solids and the flow valve of liquid; wherein, in the stirring process, metal ions in the sludge are dissolved, and the main reaction equation is as follows:
Ni(OH)2+2HCl＝NiCl2+2H2O
Cr(OH)3+3HCl＝CrCl3+3H2O
Al(OH)3+3HCl＝AlCl3+3H2O
Fe(OH)3+3HCl＝FeCl3+3H2O
Ca(OH)2+2HCl＝CaCl2+2H2O
Mg(OH)2+2HCl＝MgCl2+2H2O
and then carrying out filter pressing on the obtained solid-liquid mixture, wherein the slag yield is about 1 percent, and obtaining filtrate and filter residue. The main components of the size-mixing filter-pressing residue are a flocculating agent, namely Polyacrylamide (PAM), and a part of insoluble calcium salt contained in the raw sludge.
(B) Extracting, namely preheating the extracting agent and the filtrate obtained in the step (A) in an electric heating reaction kettle respectively, and then introducing the preheated extracting agent and the filtrate into an extraction system respectively for mixing and stirring reaction;
wherein the volume ratio of the filtrate to the extracting agent is 1: 1.25-1: 1.65, the filtrate enters from a heavy phase feed inlet of the centrifugal extractor, and the extractant enters from a light phase feed inlet of the centrifugal extractor; wherein the extracting agent is prepared by mixing 30% of P507, 60% of sulfonated kerosene and 10% of normal octane by volume fraction, adding sodium hydroxide until the saponification rate is 30-50%, mixing with the filtrate, stirring, reacting and extracting; wherein P is507 is 2-ethylhexyl phosphate, CAS NO:14802-03-0, formula: (C)8H17)2HPO3The general molecular formula is HA; wherein the extraction reaction equation in the extraction system is as follows:
NiCl2+2(HA)2＝Ni(HA2)2+2HCl
CrCl3+3(HA)2＝Cr(HA2)3+3HCl
AlCl3+3(HA)2＝Al(HA2)3+3HCl
all the raw materials are industrial pure, and a loaded organic phase and a final raffinate are obtained after extraction.
The extraction process can adopt single-stage extraction or cascade extraction, and when the concentration of the ions to be recovered in the filtrate obtained in the step (A) is higher, cascade extraction is adopted, and as shown in the figure, two or more centrifugal extractors are connected in series to carry out cascade countercurrent extraction.
And (3) filtrate enters from a heavy phase inlet of the first-stage centrifugal extractor, the filtrate after the first-stage extraction flows out from a heavy phase outlet, flows to a heavy phase inlet of the next-stage centrifugal extractor through a pipeline for repeated extraction, and flows out from a heavy phase outlet of the last-stage centrifugal extractor of the extraction system after being repeatedly extracted by the n-stage centrifugal extractor to obtain final raffinate, wherein the final raffinate can be further pumped into the acid leaching process in the step (A) for use.
And the extractant is opposite, the extractant needs to enter from the light phase inlet of the last-stage centrifugal extractor, flows out from the light phase outlet to the light phase inlet of the last-stage centrifugal extractor, and flows out from the light phase outlet of the first-stage centrifugal extractor of the extraction system after being repeatedly used to obtain a loaded organic phase.
The flow ratio R in the cascade extraction process is controlled to be 0.8, namely the ratio of the flow of an organic phase (an extractant) to the flow of a filtrate in the extraction process; the temperature of the filtrate in the extraction system is controlled at 40-45 deg.C, and the temperature of the organic phase is controlled at 38-42 deg.C.
(C) Stripping, namely feeding the loaded organic phase obtained in the step (B) into a stripping system, and stripping by adopting 31 wt% of industrial hydrochloric acid;
wherein the back-extraction reaction equation in the back-extraction system is as follows:
Al(HA2)3+3HCl＝AlCl3+3(HA)2
Ni(HA2)2+2HCl＝NiCl2+2(HA)2
Cr(HA2)3+3HC＝CrCl3+3(HA)2
and in the first section of centrifugal extractor, 31 wt% of industrial hydrochloric acid and water are added into a heavy phase inlet, the pH value of the mixed phase is controlled to be 2.0-2.5, and the hydrochloric acid reversely extracts aluminum ions loaded in the extractant to obtain an aluminum chloride solution.
And in the second section of centrifugal extractor, 31 wt% of industrial hydrochloric acid and water are added into a heavy phase inlet, the pH value of the mixed phase is controlled to be 2.8-3.5, and the hydrochloric acid reversely extracts nickel ions loaded in the extractant to obtain a nickel chloride solution.
And in the third centrifugal extractor, 31 wt% of industrial hydrochloric acid and water are added into a heavy phase inlet, the pH value of the mixed phase is controlled to be 4.0, and the hydrochloric acid reversely extracts chromium ions loaded in the extracting agent to obtain a chromium chloride solution.
The rotating speed of each centrifugal extractor in the back extraction stage is based on 2800 revolutions per minute, and a frequency converter is arranged to regulate the speed according to the concentration of filtrate in the extraction process.
And (3) leading out an aluminum chloride solution, a nickel chloride solution and a chromium chloride solution at the different stages of the back extraction system, and also obtaining back extraction wastewater and a residual organic phase.
The residual organic phase after stripping can be directly refluxed into the extraction system to be reused as an extractant, as shown in the figure. The back extraction waste water is a mixed liquid of unrecovered solutions of calcium chloride, magnesium chloride, ferric chloride and the like, does not contain metal ions harmful to the environment, and can be discharged after reaching the standard through neutralization, precipitation and filter residue.
In the process of the embodiment, the reaction time of each stage of cascade extraction and back extraction is 5-8 minutes, the total of 40 stages from extraction to back extraction, the processes such as pulp dissolving and the like are integrated, and the operation time of the whole process is 3.5-5.5 hours. The recovery rate of aluminum, nickel and chromium ions in the sludge can reach 99 percent after the serial extraction and the back extraction.
Claims (9)
1. A sludge recycling process in aluminum profile processing is characterized by comprising the following steps:
(A) slurry mixing, which comprises the steps of putting sludge generated in the aluminum profile processing into a reaction kettle for acid leaching and filter pressing;
wherein, the acid leaching adopts 31 wt% industrial hydrochloric acid, the hydrochloric acid and the sludge are proportioned according to the volume ratio of 2:1, then the mixture is added into a reaction kettle, water is added after the stirring, and the stirring and the dissolution are continued until the liquid-solid volume ratio is 500; wherein, in the stirring process, metal ions in the sludge are dissolved, and the main reaction equation is as follows:
Ni(OH)2+2HCl＝NiCl2+2H2O
Cr(OH)3+3HCl＝CrCl3+3H2O
Al(OH)3+3HCl＝AlCl3+3H2O
Fe(OH)3+3HCl＝FeCl3+3H2O
Ca(OH)2+2HCl＝CaCl2+2H2O
Mg(OH)2+2HCl＝MgCl2+2H2O
then carrying out filter pressing on the obtained solid-liquid mixture to obtain filtrate and filter residue;
(B) extracting, namely preheating the extracting agent and the filtrate obtained in the step (A) in an electric heating reaction kettle respectively, then introducing the preheated extracting agent and the filtrate into an extraction system respectively for mixing, stirring and reacting, wherein the temperature of the filtrate in the extraction system is controlled to be 40-45 ℃, and the temperature of an organic phase is controlled to be 38-42 ℃;
wherein the volume ratio of the filtrate to the extracting agent is 1: 1.25-1: 1.65, the filtrate enters from a heavy phase feed inlet of the centrifugal extractor, and the extractant enters from a light phase feed inlet of the centrifugal extractor; wherein the extracting agent is prepared by mixing 30 percent of P507, 60 percent of sulfonated kerosene and 10 percent of normal octane by volume fraction and adding sodium hydroxide to reach the saponification rate of 30 to 50 percent; wherein the P507 is 2-ethylhexyl phosphate 2-ethylhexyl ester with a general molecular formula of HA; wherein the extraction reaction equation in the extraction system is as follows:
NiCl2+2(HA)2＝Ni(HA2)2+2HCl
CrCl3+3(HA)2＝Cr(HA2)3+3HCl
AlCl3+3(HA)2＝Al(HA2)3+3HCl
obtaining a loaded organic phase and a final raffinate after extraction;
(C) stripping, namely feeding the loaded organic phase obtained in the step (B) into a stripping system, and stripping by adopting 31 wt% of industrial hydrochloric acid;
wherein the back-extraction reaction equation in the back-extraction system is as follows:
Al(HA2)3+3HCl＝AlCl3+3(HA)2
Ni(HA2)2+2HCl＝NiCl2+2(HA)2
Cr(HA2)3+3HC＝CrCl3+3(HA)2
a first-stage centrifugal extractor, wherein 31 wt% of industrial hydrochloric acid and water are added into a heavy phase inlet, the pH value of a mixed phase is controlled to be 2.0-2.5, and aluminum ions loaded in an extractant are back-extracted by the hydrochloric acid to obtain an aluminum chloride solution;
a second-stage centrifugal extractor, wherein 31 wt% of industrial hydrochloric acid and water are added into a heavy phase inlet, the pH value of a mixed phase is controlled to be 2.8-3.5, and the hydrochloric acid reversely extracts nickel ions loaded in an extractant to obtain a nickel chloride solution;
a third section of centrifugal extractor, wherein 31 wt% of industrial hydrochloric acid and water are added into a heavy phase inlet, the pH value of a mixed phase is controlled to be 4.0, and chromium ions loaded in an extracting agent are back extracted by the hydrochloric acid to obtain a chromium chloride solution;
and (3) leading out an aluminum chloride solution, a nickel chloride solution and a chromium chloride solution at the different stages of the back extraction system, and also obtaining back extraction wastewater and a residual organic phase.
2. The process for recycling sludge in the processing of aluminum profiles as claimed in claim 1, wherein in the acid leaching process in the step (A), after adding hydrochloric acid and sludge into the reaction kettle, stirring is carried out for 10 minutes, and then water is added for continuous stirring.
3. The process for recycling sludge in the processing of aluminum profiles as set forth in claim 1, wherein the extraction process of the step (B) can adopt single-stage extraction or cascade extraction.
4. The process for recycling sludge in the processing of aluminum profiles as claimed in claim 3, wherein when the step (B) adopts cascade extraction, at least two centrifugal extractors are connected in series to carry out cascade countercurrent extraction;
wherein the filtrate obtained in the step (A) enters from a heavy phase inlet of a first-stage centrifugal extractor, the filtrate subjected to first-stage extraction flows out from a heavy phase outlet, flows to a heavy phase inlet of a next-stage centrifugal extractor through a pipeline for repeated extraction, and flows out from a heavy phase outlet of a last-stage centrifugal extractor of an extraction system after being repeatedly extracted by an n-stage centrifugal extractor to obtain final raffinate;
the extractant enters from the light phase inlet of the last stage of centrifugal extractor, flows out from the light phase outlet to the light phase inlet of the last stage of centrifugal extractor, and flows out from the light phase outlet of the first stage of centrifugal extractor of the extraction system after being repeatedly used, so as to obtain a loaded organic phase.
5. The process for recycling sludge in the processing of aluminum profiles as set forth in claim 4, wherein the flow ratio R of the flow of the organic phase to the flow of the filtrate in the cascade extraction process is controlled to be 0.8.
6. The process for recycling sludge in the processing of aluminum profiles as claimed in claim 4, wherein the reaction time of each stage in the cascade extraction process is 5-8 minutes.
7. The process for recycling sludge in the aluminum profile processing according to claim 1, wherein the final raffinate obtained in the step (B) can be continuously pumped into the acid leaching process in the step (A) for use.
8. The process for recycling sludge in the processing of aluminum profiles as claimed in claim 1, wherein the residual organic phase obtained in the step (C) can be directly returned to the extraction system for reuse as an extractant.
9. The process for recycling sludge in the processing of aluminum profiles as claimed in claim 1, wherein the reaction time of each stage in the back extraction process of the step (C) is 5-8 minutes.
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