CN111204780B - Resource utilization process of salt mud in chlor-alkali industry - Google Patents
Resource utilization process of salt mud in chlor-alkali industry Download PDFInfo
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- CN111204780B CN111204780B CN202010020527.6A CN202010020527A CN111204780B CN 111204780 B CN111204780 B CN 111204780B CN 202010020527 A CN202010020527 A CN 202010020527A CN 111204780 B CN111204780 B CN 111204780B
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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
- C01F5/00—Compounds of magnesium
- C01F5/14—Magnesium hydroxide
- C01F5/22—Magnesium hydroxide from magnesium compounds with alkali hydroxides or alkaline- earth oxides or hydroxides
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D3/00—Halides of sodium, potassium or alkali metals in general
- C01D3/04—Chlorides
- C01D3/08—Preparation by working up natural or industrial salt mixtures or siliceous minerals
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/41—Preparation of salts of carboxylic acids
- C07C51/412—Preparation of salts of carboxylic acids by conversion of the acids, their salts, esters or anhydrides with the same carboxylic acid part
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/42—Separation; Purification; Stabilisation; Use of additives
- C07C51/47—Separation; Purification; Stabilisation; Use of additives by solid-liquid treatment; by chemisorption
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
- C01P2006/00—Physical properties of inorganic compounds
- C01P2006/80—Compositional purity
Abstract
A process for reclaiming the salt mud in chlor-alkali industry includes such steps as dissolving out Ca, Mg and other metal elements from the salt mud by hydrochloric acid, and extracting high-purity Ca oxalate and Mg hydroxide step by step. The method comprises the following specific steps: firstly, drying salt slurry, and grinding the salt slurry by using a ball mill to obtain salt slurry powder; then, washing the salt slurry powder with softened water to remove water-soluble impurities in the powder; secondly, carrying out acid washing treatment on the washed salt mud by using hydrochloric acid to extract calcium, magnesium and other acid-soluble salts in the salt mud; and finally, sequentially adding oxalic acid solution and sodium hydroxide solution into the pickling solution to respectively obtain high-purity calcium oxalate and high-purity magnesium hydroxide. The method has simple process operation and short flow, realizes the resource utilization of calcium and magnesium while reducing the industrial salt slurry by more than 90 percent, and provides a feasible scheme for the reduction treatment and the resource utilization of the salt slurry solid waste in the chlor-alkali industry.
Description
Technical Field
The invention relates to a solid waste treatment and disposal technology, in particular to a resource utilization technology of salt mud waste produced in the chlor-alkali industry, belonging to the technical field of environment.
Background
With the development of the chlor-alkali industry, more and more salty mud is produced during brine refining, and 98.5% of salty mud produced every day is directly discharged without any treatment, which is calculated by 350 ten thousand tons of caustic soda produced nationwide at present. Salt mud is discharged at 350 ten thousand cubic meters per year. A large amount of salt mud is directly discharged, so that environmental pollution is caused and ecological health is harmed. Therefore, the salt mud treatment and resource utilization process technology development are carried out, the environmental influence of the salt mud is eliminated, and the method has important environmental benefit and social benefit.
Due to the pollution of the salt mud to the environment, many domestic units have carried out many researches on the comprehensive utilization of the salt mud, such as: the Renhai electrochemical plant and Guangzhou chemical plant have carried out salt mud to prepare light MgCO in the 70 s3The test of (1); the 1980 east chemical industry institute uses salt mud as raw material, successfully carries out the pilot plant of factory carbonization method for preparing light MgO, and later cooperates with Shanghai electrochemical plant to realize industrialization of the process, but the process has the problems of low MgO yield, complex process, high energy consumption and the like, so that the further promotion of factory application is difficult; aiming at the problem of high mercury content in the wide salt mud, a Tianjin chemical plant builds a project for recovering mercury from the salt mud; the stanza chemical plant aims at the Ba (SO) in the salt mud of the plant4In the case of high content, Ba (SO) is recovered from the salty mud4The study of (1); the Shanghai Nature chemical plant proposes that the salt mud and the calcium carbide paste are pressed dry together and then used for paving, and the method can treat the salt mud more thoroughly but cannot utilize the effective components of the salt mud.
Therefore, reduction and resource utilization are feasible ideas for reducing the treatment cost of the salty mud and improving the environmental benefit. The calcium and magnesium content in the salt mud produced in the chlor-alkali industry is high, the calcium and magnesium content in the salt mud is dissolved out in an acid washing mode, and the Ca content in the acid washing solution is increased in an oxalic acid adding mode2+Converted into calcium oxalate crystals with higher purity, and Mg2+Then adding sodium hydroxide for precipitation to prepare magnesium hydroxide with higher purity, which can be used as excellent flame retardant for plastic and rubber products, acid inhibitor and laxative agent in medicine, and the like. Both calcium oxalate and magnesium hydroxide have good economic value. At present, the market price of industrial calcium oxalate is 15000-17000 yuan/ton, and the market price of magnesium hydroxide is 5000 yuan/ton. The method can obtain the valuable calcium oxalate and magnesium hydroxide products while realizing the reduction of the salt mud, and has important commercial value.
Disclosure of Invention
Aiming at the defects of the prior art for recycling the salt slurry, the invention aims to provide a process for recycling the salt slurry in the chlor-alkali industry, which can realize the reduction of the salt slurry and the recycling of main components such as calcium, magnesium and the like.
According to the above purpose, the technical principle of the technical scheme of the invention is as follows:
extracting Ca from salt mud by hydrochloric acid pickling2+、Mg2+And ions are added, and high-purity calcium oxalate and high-purity magnesium hydroxide are extracted step by step in a mode of sequentially adding oxalic acid and sodium hydroxide, so that the resource utilization of calcium and magnesium in the salt mud is realized.
In order to solve the problems, the invention adopts the following technical scheme:
1) pretreatment: drying the salt slurry, controlling the water content within 5%, and crushing to obtain salt slurry powder with the average particle size of 30-50 microns;
2) washing with water: cleaning the salt slurry powder by using softened water, wherein the volume ratio of water to solid is controlled to be 2-4: 1;
3) acid washing: adding concentrated hydrochloric acid into the washed salt slurry suspension to extract calcium and magnesium ions in the salt slurry;
4) solid-liquid separation: and (3) centrifugally separating the mixed solution after the acid washing to obtain salt mud residues and an aqueous solution rich in calcium, magnesium and other ions. The weight of the salt mud residue is reduced by more than 90 percent compared with that of the salt mud;
5) and (3) recovering calcium oxalate: adding a proper amount of oxalic acid solution into the separated aqueous solution, and filtering through a filter membrane with the aperture of 0.45 mu m to recover calcium oxalate;
6) recovering magnesium hydroxide: and adding a proper amount of sodium hydroxide solution into the solution after the calcium oxalate is recovered, and recovering the magnesium hydroxide after filtering the solution by a filter membrane with the aperture of 0.45 mu m.
Preferably, in the step 1), the drying temperature of the salty mud is 80-90 ℃, and the moisture content of the salty mud can be reduced to below 5% within 4 hours. When the temperature is lower than 80 ℃, the moisture content of the salt slurry can be reduced to below 5 percent only by drying for more than 24 hours, and the drying efficiency is influenced; and the temperature is higher than 90 ℃, a compact protective film is easily formed on the surface layer of the salt mud to influence the water dispersion and the energy utilization efficiency. The crushing treatment is grinding by a ball mill.
Preferably, the dust-containing gas generated in the crushing treatment process is collected and sent to a water washing link; and collecting the acidic steam generated in the acid washing process, and sending the acidic steam into a water washing link. The salt mud and the hydrochloric acid are fully utilized while the environmental pollution is avoided.
Preferably, hydrochloric acid is used as the pickling solution in the step 3), and other types of acids such as nitric acid, sulfuric acid and the like cannot be used. If nitric acid is used as a pickling agent, the effect of the nitric acid is the same as that of hydrochloric acid, the volume of the salt mud can be reduced by more than 90%, but the nitric acid is unstable, is easy to decompose when exposed to light, is not suitable for conventional production links, and nitrate radicals have strong oxidizing property, damage the structure of oxalic acid, and can not recover calcium oxalate in an acidic environment. The sulfuric acid also has strong oxidizing property, and after being mixed with the salt slurry, black suspension floccules can be generated due to the existence of interfering ions in the pickling solution, and the volume of the pickled sulfuric acid is only reduced by about 10 percent, and the sulfuric acid also has strong oxidizing property and is not beneficial to the recovery of calcium oxalate. Other types of acid are adopted, high-concentration acid radical wastewater is generated, and the wastewater is difficult to discharge after reaching the standard. The hydrochloric acid acidification is beneficial to the reduction of salt mud and the subsequent calcium and magnesium recovery, and the finally generated high-concentration acid radical wastewater, namely the sodium chloride wastewater can be reused as a raw material for the production of the chlor-alkali industry after being concentrated.
Preferably, the mass concentration of the hydrochloric acid washing solution is 40-50% so as to effectively control the volume of the washing solution. According to the content of calcium and magnesium in the salt mud and the composition of minerals, the adding amount of the hydrochloric acid is determined to be 1.4-1.5 mL (hydrochloric acid)/g (salt mud).
Preferably, the acid washing mixed liquor in the step 4) has high salt content and is thick. If natural sedimentation is adopted, the mixed pickling liquid is layered after 3-5 hours, fine suspended particles exist in the supernatant, the turbidity is 1.2NTU, the solid-liquid separation time is long, and the effect is poor; if qualitative filter paper and suction filtration equipment are adopted for solid-liquid separation, the separation operation can be completed only within 2.5-3.5 h by using the acidic mixed solution, the turbidity of the filtered pickling solution is 0.1NTU, the separation effect is good, but the time is long, the problem of serious membrane pollution exists, and continuous production is difficult to realize. And selecting a centrifugal separation technology, wherein the centrifugal time is 4-5 min under the condition of the rotating speed of 4000-5000 r/min, the residue and the clear liquid in the pickling mixed liquid can be effectively separated, and the turbidity of the clear liquid is 0.2NTU, so the centrifugal separation technology is the optimal means for carrying out solid-liquid separation on the pickling mixed liquid.
Preferably, Ca in the clarified acid washing solution obtained in the step 4)2+The content is 20.3g/L to 30.0g/L, Mg2+4.0 g/L-5.0 g/L of Na+2.0 g/L-3.0 g/L, Sr2+0.5g/L to 0.74g/L, Fe3+0.46g/L to 0.67g/L of Al3+0.32g/L to 0.48g/L, Mn2+0.12g/L to 0.18g/L, PO4 3-0.02 g/L-0.04 g/L, high content of coexisting ions and complex components;
preferably, in the step 5), the concentration of the oxalic acid solution added into the pickling solution containing various heavy metal ions is 0.5-0.6 mol/L, the pH of the pickling solution is controlled within the range of 4.0-6.0, and the residual Ca in the pickling solution is controlled2+The content is 100 mg/L-200 mg/L, so as to prevent other coexisting cations from precipitating and influencing the purity of the calcium oxalate powder;
preferably, in the step 5), after the calcium oxalate is completely precipitated, a filtration device is adopted to realize the rapid solid-liquid separation through a filter membrane with the aperture of 0.45 μm;
preferably, in the step 5), the obtained calcium oxalate solid needs to be naturally air-dried under a dark condition or dried in an oven at 20 ℃ for 48 hours;
preferably, in the step 6), Ca is recovered2+Adding sodium hydroxide solution into the pickling solution, wherein the concentration of the sodium hydroxide solution is 0.5mol/L, adjusting the pH value of the pickling solution to 7.5-8.5, and precipitating Mg2+Post-control of residual Mg in liquid phase2+The content is 50-100 mg/L, and high-purity magnesium hydroxide can be obtained;
preferably, in the step 6), after the magnesium hydroxide precipitate is generated, solid-liquid rapid separation can be realized by using a filtration membrane with the aperture of 0.45 μm through suction filtration equipment;
preferably, in the step 6), the rest acid-washing wastewater contains high-concentration NaCl, and can be concentrated and recycled to be used as a raw material in the chlor-alkali industry.
The invention has the advantages that:
the method provided by the invention is simple to operate and short in flow, can fully recover calcium and magnesium components in the salt slurry while realizing the reduction of the solid salt slurry waste produced in the chlor-alkali industry, changes waste into valuable, reduces the environmental pollution caused by waste discharge, and can obtain calcium oxalate and magnesium hydroxide which can be used as industrial raw materials with high value.
Drawings
FIG. 1 is a process flow diagram for resource utilization of salt mud in chlor-alkali industry provided by the invention.
FIG. 2 is a schematic diagram of the calcium oxalate product separated according to the present invention.
FIG. 3 is a schematic diagram of the magnesium hydroxide product separated according to the present invention.
Detailed Description
The embodiments of the present invention will be described in detail below with reference to the drawings and examples.
Referring to fig. 1, the invention relates to a resource utilization process of salt mud in chlor-alkali industry, which utilizes hydrochloric acid to dissolve calcium, magnesium and other metal elements in the salt mud and extracts high-purity calcium oxalate and magnesium hydroxide step by step. The method comprises the following specific steps: firstly, drying salt slurry, and grinding the salt slurry by using a ball mill to obtain salt slurry powder; then, washing the salt slurry powder with softened water; secondly, carrying out acid washing treatment on the washed salt mud by using hydrochloric acid to dissolve out calcium, magnesium and other acid-soluble salts in the salt mud; and finally, sequentially adding oxalic acid and sodium hydroxide into the pickling solution to finally obtain high-purity calcium oxalate and high-purity magnesium hydroxide.
In a specific embodiment of the invention, the salt mud selected in the experiment is from salt mud produced by a chlor-alkali chemical industry of Jiangsu, and the water content of the salt mud is known to be 35-40%, and the treatment steps are as follows.
(1) Drying wet salt mud at 80 ℃ for 4h, crushing the wet salt mud by using a ball mill to obtain a 5.2g salt mud powder sample, wherein the particle size of the salt mud powder sample is 35-50 mu m, and the main elements of the original salt mud are shown in table 1 through detection, so that the salt mud has complex components;
table 1: full-rock index element analysis of salt mud
| Element type | Content% | Element type | Content% |
| Oxygen (O) | 27.5 | Aluminum (Al) | 0.017 |
| Calcium (Ca) | 22.4 | Barium (Ba) | 0.005 |
| Sodium (Na) | 10.1 | Lead (Pb) | 0.002 |
| Chlorine (Cl) | 8.77 | Zinc (Zn) | 0.002 |
| Silicon (Si) | 3.78 | Copper (Cu) | 0 |
| Magnesium (Mg) | 1.07 | Arsenic (As) | 0 |
| Iron (Fe) | 0.20 | Cobalt (Co) | 0 |
| Sulfur (S) | 0.16 | Cadmium (Cd) | 0 |
| Potassium (K) | 0.12 | Mercury (Hg) | 0 |
| Manganese (Mn) | 0.08 | Molybdenum (Mo) | 0 |
| Phosphorus (P) | 0.03 |
(2) Mixing the salt mud powder obtained in the step (1) with 15mL of pure water to form suspension, and washing with water;
(3) and (3) adding 7.5mL of hydrochloric acid (12mol/L) into the suspension obtained in the step (2) for acid washing, and finishing the acid washing stage when the gas production process is terminated to obtain an acid washing mixed solution.
(4) And centrifugally separating to obtain the salt mud residue and the pickling solution respectively. After drying and weighing, the weight of the treated salty mud can be reduced by 90.2%, and the main cation content in the liquid measured after acid washing is shown in table 2, and the components are complex.
TABLE 2 main cation species and contents in pickling solution
(3) The pH of the system was controlled to about 4.5 and the residual amount of calcium ions was controlled to about 100mg/L, and 50mL of oxalic acid solution (0.58mol/L) was added to the acid wash. In order to ensure the purity of the obtained calcium oxalate, the concentration of the added oxalic acid solution needs to be controlled, and the reaction system is rapidly stirred (150-250 r/min) at the same time, so that the phenomenon of overhigh local concentration of oxalic acid is avoided. And filtering and naturally drying to obtain 2.7g of calcium oxalate product, wherein the obtained calcium oxalate product has uniform particles, is light yellow (shown in figure 2) and has the purity of more than 98 percent.
(4) The pH of the system was controlled to about 8.0 and the residual amount of magnesium ions was controlled to about 100mg/L, and 33.4mL of a sodium hydroxide solution (0.5mol/L) was added to the pickling solution from which calcium ions were recovered in step (3). In order to ensure the purity of the obtained magnesium hydroxide, the concentration of the added sodium hydroxide solution needs to be controlled, and the reaction system is rapidly stirred (150-250 r/min) to avoid the phenomenon of overhigh local alkali concentration. After filtration through a 0.45 μm filter membrane and drying, 0.4g of magnesium hydroxide product was obtained (see FIG. 3). The obtained magnesium hydroxide has fine particles and the purity of more than 98 percent.
From the results, the process can obtain high-purity calcium oxalate and magnesium hydroxide products, and can realize the recycling of the salt mud waste.
Claims (7)
1. A resource utilization process of salt mud in chlor-alkali industry is characterized by comprising the following steps:
1) pretreatment: the salt mud is derived from salt mud produced by a chlor-alkali chemical industry enterprise in Jiangsu, is dried, the water content is controlled within 5%, and then is crushed to obtain salt mud powder with the average particle size of 30-50 mu m, wherein the whole rock index element analysis of the salt mud is as follows:
2) Washing with water: cleaning the salt slurry powder by using softened water, wherein the volume ratio of water to solid is controlled to be 2-4: 1;
3) acid washing: adding concentrated hydrochloric acid into the washed salt slurry suspension for acid washing to extract calcium and magnesium ions in the salt slurry, and finishing the acid washing stage when the gas production process is finished;
4) solid-liquid separation: carrying out centrifugal separation on the mixed solution after acid washing to obtain salt mud residues and an aqueous solution rich in calcium and magnesium ions, wherein the weight of the salt mud residues is reduced by more than 90% compared with that of the salt mud, the centrifugal separation is carried out for 4-5 min under the condition of the rotating speed of 4000-5000 r/min, the residues and the clear solution in the mixed solution after acid washing are effectively separated, and the turbidity of the clear solution is 0.2 NTU;
5) and (3) recovering calcium oxalate: adding a proper amount of oxalic acid solution into the separated water solution, wherein the concentration of the oxalic acid solution is 0.5-0.6 mol/L, the pH of the pickling solution is controlled to be 4.0-6.0, and the residual Ca in the pickling solution is controlled2+The content is 100 mg/L-200 mg/L, so as to prevent other coexisting cations from precipitating and influencing the purity of the calcium oxalate powder; after the calcium oxalate is completely precipitated, the solid-liquid rapid separation is realized by adopting suction filtration equipment through a filter membrane with the aperture of 0.45 mu m, the obtained calcium oxalate product has uniform particles and the purity of more than 98 percent;
6) recovering magnesium hydroxide: adding a sodium hydroxide solution into the solution after the calcium oxalate is recovered, wherein the concentration of the sodium hydroxide solution is 0.5mol/L, adjusting the pH value of the pickling solution to be 7.5-8.5, and precipitating Mg2+Post-control of residual Mg in liquid phase2+The content is 50-100 mg/L, the magnesium hydroxide is recovered after being filtered by a filter membrane with the aperture of 0.45 mu m, the obtained magnesium hydroxide particles are fine, and the purity is more than 98%.
2. The resource utilization process of the salt mud in the chlor-alkali industry as claimed in claim 1, wherein in step 1), the drying temperature of the salt mud is in the range of 80 ℃ to 90 ℃, the water content of the salt mud is reduced to below 5% within 4h, and the crushing treatment is carried out by using a ball mill.
3. The resource utilization process of the salt mud in the chlor-alkali industry as claimed in claim 1, wherein the dust-containing gas generated in the crushing process is collected and sent to a water washing step; and collecting the acidic steam generated in the acid washing process, and sending the acidic steam into a water washing link.
4. The resource utilization process of the salt mud in the chlor-alkali industry as claimed in claim 1, wherein the mass concentration of the hydrochloric acid washing solution in the step 3) is 40% -50%, and according to the contents of calcium and magnesium in the salt mud and the mineral composition, the hydrochloric acid: the adding amount of the hydrochloric acid is determined according to the proportion of 1.4-1.5 mL/g of the salt mud.
5. The resource utilization process of the salt mud in the chlor-alkali industry as claimed in claim 1, wherein in step 4), Ca in the pickling solution is added2+The content is 20.3g/L to 30.0g/L, Mg2+4.0 g/L-5.0 g/L of Na+2.0 g/L-3.0 g/L, Sr2+0.5g/L to 0.74g/L, Fe3+0.46g/L to 0.67g/L of Al3+0.32g/L to 0.48g/L, Mn2+0.12g/L to 0.18g/L, PO4 3﹣Is 0.02g/L to 0.04 g/L.
6. The resource utilization process of the salt mud in the chlor-alkali industry as claimed in claim 1, wherein in said step 5), the obtained calcium oxalate solid is air dried naturally under the dark condition or dried in an oven at 20 ℃ for 48 h.
7. The resource utilization process of the salty mud in the chlor-alkali industry as recited in claim 1, wherein in said step 6), after the magnesium hydroxide precipitate is generated, a filtration device is used to realize the solid-liquid rapid separation through a filter membrane with a pore size of 0.45 μm, and the acid washing wastewater after calcium and magnesium recovery contains high concentration NaCl, which is concentrated and recovered for use as the raw material in the chlor-alkali industry.
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| CN113089076B (en) * | 2021-03-17 | 2022-04-22 | 西安交通大学 | Method for preparing calcium sulfate whiskers based on chlor-alkali salt mud |
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