CN114368867A - Treatment process and method for high-concentration salt aquatic product crystal salt of coal-to-liquid - Google Patents
Treatment process and method for high-concentration salt aquatic product crystal salt of coal-to-liquid Download PDFInfo
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- CN114368867A CN114368867A CN202111639853.6A CN202111639853A CN114368867A CN 114368867 A CN114368867 A CN 114368867A CN 202111639853 A CN202111639853 A CN 202111639853A CN 114368867 A CN114368867 A CN 114368867A
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- 150000003839 salts Chemical class 0.000 title claims abstract description 78
- 239000007788 liquid Substances 0.000 title claims abstract description 67
- 238000000034 method Methods 0.000 title claims abstract description 49
- 230000008569 process Effects 0.000 title claims abstract description 23
- 239000013078 crystal Substances 0.000 title claims description 85
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims abstract description 136
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 claims abstract description 86
- VWDWKYIASSYTQR-UHFFFAOYSA-N sodium nitrate Chemical compound [Na+].[O-][N+]([O-])=O VWDWKYIASSYTQR-UHFFFAOYSA-N 0.000 claims abstract description 86
- 229910052938 sodium sulfate Inorganic materials 0.000 claims abstract description 86
- 235000011152 sodium sulphate Nutrition 0.000 claims abstract description 86
- 238000002425 crystallisation Methods 0.000 claims abstract description 83
- 230000008025 crystallization Effects 0.000 claims abstract description 83
- 239000011780 sodium chloride Substances 0.000 claims abstract description 68
- 239000012267 brine Substances 0.000 claims abstract description 64
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims abstract description 64
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims abstract description 60
- 235000010344 sodium nitrate Nutrition 0.000 claims abstract description 43
- 239000004317 sodium nitrate Substances 0.000 claims abstract description 43
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 40
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims abstract description 22
- 239000000047 product Substances 0.000 claims abstract description 21
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 claims abstract description 20
- 239000002244 precipitate Substances 0.000 claims abstract description 20
- 238000001179 sorption measurement Methods 0.000 claims abstract description 20
- 239000002351 wastewater Substances 0.000 claims abstract description 14
- 229910000029 sodium carbonate Inorganic materials 0.000 claims abstract description 11
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 claims abstract description 10
- 229910000019 calcium carbonate Inorganic materials 0.000 claims abstract description 10
- 229910001424 calcium ion Inorganic materials 0.000 claims abstract description 10
- 238000003756 stirring Methods 0.000 claims abstract description 10
- 239000002002 slurry Substances 0.000 claims description 72
- 239000012452 mother liquor Substances 0.000 claims description 63
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 58
- 238000000909 electrodialysis Methods 0.000 claims description 36
- 238000001223 reverse osmosis Methods 0.000 claims description 36
- 238000000108 ultra-filtration Methods 0.000 claims description 27
- 230000008719 thickening Effects 0.000 claims description 24
- 238000000926 separation method Methods 0.000 claims description 21
- 239000000243 solution Substances 0.000 claims description 20
- 238000001035 drying Methods 0.000 claims description 19
- GNFTZDOKVXKIBK-UHFFFAOYSA-N 3-(2-methoxyethoxy)benzohydrazide Chemical compound COCCOC1=CC=CC(C(=O)NN)=C1 GNFTZDOKVXKIBK-UHFFFAOYSA-N 0.000 claims description 18
- FGUUSXIOTUKUDN-IBGZPJMESA-N C1(=CC=CC=C1)N1C2=C(NC([C@H](C1)NC=1OC(=NN=1)C1=CC=CC=C1)=O)C=CC=C2 Chemical compound C1(=CC=CC=C1)N1C2=C(NC([C@H](C1)NC=1OC(=NN=1)C1=CC=CC=C1)=O)C=CC=C2 FGUUSXIOTUKUDN-IBGZPJMESA-N 0.000 claims description 18
- 239000000706 filtrate Substances 0.000 claims description 18
- 238000001704 evaporation Methods 0.000 claims description 17
- 230000008020 evaporation Effects 0.000 claims description 17
- 238000001816 cooling Methods 0.000 claims description 16
- 239000000446 fuel Substances 0.000 claims description 11
- YTAHJIFKAKIKAV-XNMGPUDCSA-N [(1R)-3-morpholin-4-yl-1-phenylpropyl] N-[(3S)-2-oxo-5-phenyl-1,3-dihydro-1,4-benzodiazepin-3-yl]carbamate Chemical compound O=C1[C@H](N=C(C2=C(N1)C=CC=C2)C1=CC=CC=C1)NC(O[C@H](CCN1CCOCC1)C1=CC=CC=C1)=O YTAHJIFKAKIKAV-XNMGPUDCSA-N 0.000 claims description 9
- 239000000084 colloidal system Substances 0.000 claims description 9
- 239000013505 freshwater Substances 0.000 claims description 9
- 239000007921 spray Substances 0.000 claims description 9
- 238000003860 storage Methods 0.000 claims description 9
- 239000006228 supernatant Substances 0.000 claims description 9
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 6
- 239000002562 thickening agent Substances 0.000 claims description 6
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 3
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 3
- SOCTUWSJJQCPFX-UHFFFAOYSA-N dichromate(2-) Chemical compound [O-][Cr](=O)(=O)O[Cr]([O-])(=O)=O SOCTUWSJJQCPFX-UHFFFAOYSA-N 0.000 claims description 3
- 150000002391 heterocyclic compounds Chemical class 0.000 claims description 3
- 229910052757 nitrogen Inorganic materials 0.000 claims description 3
- 229910052760 oxygen Inorganic materials 0.000 claims description 3
- 239000001301 oxygen Substances 0.000 claims description 3
- 239000002957 persistent organic pollutant Substances 0.000 claims description 3
- 150000002989 phenols Chemical class 0.000 claims description 3
- -1 polycyclic aromatic compounds Chemical class 0.000 claims description 3
- 229920006395 saturated elastomer Polymers 0.000 claims description 3
- 229910052717 sulfur Inorganic materials 0.000 claims description 3
- 239000011593 sulfur Substances 0.000 claims description 3
- 230000009467 reduction Effects 0.000 claims description 2
- 239000000126 substance Substances 0.000 abstract description 8
- 239000003245 coal Substances 0.000 abstract description 6
- 238000005516 engineering process Methods 0.000 abstract description 4
- 230000000694 effects Effects 0.000 description 3
- 239000002920 hazardous waste Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 230000004075 alteration Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000005272 metallurgy Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000000575 pesticide Substances 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 239000010802 sludge Substances 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- 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
- C01D3/14—Purification
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D5/00—Sulfates or sulfites of sodium, potassium or alkali metals in general
- C01D5/16—Purification
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D9/00—Nitrates of sodium, potassium or alkali metals in general
- C01D9/16—Purification
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/10—Treatment of water, waste water, or sewage by heating by distillation or evaporation by direct contact with a particulate solid or with a fluid, as a heat transfer medium
- C02F1/12—Spray evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/28—Treatment of water, waste water, or sewage by sorption
- C02F1/283—Treatment of water, waste water, or sewage by sorption using coal, charred products, or inorganic mixtures containing them
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/38—Treatment of water, waste water, or sewage by centrifugal separation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/469—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis
- C02F1/4693—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis electrodialysis
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
-
- 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
- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
- Inorganic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Agronomy & Crop Science (AREA)
- Hydrology & Water Resources (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
- Water Treatment By Electricity Or Magnetism (AREA)
Abstract
The invention discloses a treatment process and a method for high-concentration salt aquatic product crystallization salt of coal-to-liquids, which comprises the following steps: step a: firstly, the strong brine passes through an activated carbon adsorption tower, the concentration of the high strong brine of the coal-to-liquids is reduced through activated carbon adsorption, and the step b: and c, adding sodium hydroxide into the coal-to-liquids high-concentration brine with the concentration reduced in the step a to enable pollution factors to form precipitates, adding sodium carbonate, stirring to enable the sodium hydroxide to fully react in the coal-to-chemicals high-concentration brine, and enabling the sodium carbonate to form calcium carbonate precipitates with the residual calcium ions. The invention realizes zero discharge of high-concentration brine by sodium chloride and sodium sulfate separated from the high-concentration brine of coal-to-liquids, well ensures the purity of the sodium chloride and the sodium sulfate, respectively crystallizes the sodium chloride, the sodium sulfate and the sodium nitrate in the high-concentration brine to reach industrial products, finally realizes the process technology of resource utilization of crystallized salt and zero discharge of wastewater, and solves the problem of non-ideal wastewater zero discharge of coal chemical industry enterprises in chemical treatment.
Description
Technical Field
The invention relates to the technical field of treatment of high-concentration brine of coal-derived fuel, in particular to a treatment process and a treatment method of high-concentration brine of coal-derived fuel for water crystallization salt production.
Background
The high-salt wastewater is wastewater with the total salt mass fraction of at least 1 percent, has wide sources and is mainly concentrated in the industries of electric power, oil refining, chemical industry, metallurgy, papermaking, pesticides and the like, wherein the coal gas, washing wastewater, circulating water system drainage, chemical water station drainage and the like in the production process of the main source of the high-salt wastewater in the coal chemical industry are characterized in that the high-salt wastewater has high salt content, most of the high-salt wastewater is Cl-, SO42-, Na + and the like, pollutants mainly comprise the total salt content, the high-salt wastewater has high density, activated sludge is easy to float and run off, the purification effect of a biological treatment system is seriously influenced, according to the high-salt water treatment condition in all coal chemical engineering projects at present, the near zero emission of high-concentration brine is realized only by a mechanical steam compression technology or a multi-effect evaporation crystallization technology, concentrated solution generated by the system is usually discharged to an evaporation pond or crystallized to generate 'mixed salt' and become dangerous waste, the limited evaporation capacity of the evaporation pond and the high treatment cost brought by the treatment of the mixed salt as hazardous waste not only bring great harm to the environment, but also greatly increase the treatment cost of the hazardous waste of enterprises, and can not meet the requirements of the current market.
Disclosure of Invention
The invention aims to provide a treatment process and a treatment method for high-concentration salt aquatic product crystallized salt of coal-made oil, which have the advantage of good treatment effect and solve the problem of poor treatment effect of the treatment process and the treatment method for the high-concentration salt aquatic product crystallized salt of the coal-made oil.
In order to achieve the purpose, the invention provides the following technical scheme: the treatment process and the method for the high-concentration salt aquatic product crystallization salt of the coal-to-liquid are characterized by comprising the following steps of: the method comprises the following steps:
step a: firstly, passing strong brine through an activated carbon adsorption tower, and reducing the concentration of the high strong brine of the coal-to-liquid fuel through activated carbon adsorption;
step b: b, adding sodium hydroxide into the coal-to-liquids high-concentration brine with the concentration reduced in the step a to enable pollution factors to form precipitates, adding sodium carbonate, stirring to enable the sodium hydroxide to fully react in the coal-to-liquids high-concentration brine, forming calcium carbonate precipitates with the remaining calcium ions, standing, and taking supernatant to obtain clear liquor;
step c: b, sequentially carrying out preheating treatment and evaporation concentration treatment on the clarified liquid obtained in the step b, carrying out sodium sulfate crystallization treatment on high-concentration brine subjected to evaporation concentration treatment to obtain sodium sulfate slurry and mother liquor, carrying out thickening and crystal growth treatment on the sodium sulfate slurry, and then carrying out centrifugal separation to obtain sodium sulfate crystals, wherein the clarified liquid is subjected to sodium sulfate crystallization treatment through cooling and temperature reduction;
step d: c, crystallizing the mother liquor obtained in the step c to obtain sodium nitrate slurry and the mother liquor, and centrifugally separating the sodium nitrate slurry to obtain sodium nitrate crystals;
step e: d, carrying out sodium chloride crystallization treatment on the mother liquor obtained in the step d to obtain sodium chloride slurry and the mother liquor, and carrying out thickening and crystal growth treatment on the obtained sodium chloride slurry and then carrying out centrifugal separation to obtain sodium chloride crystals;
step f: e, performing ultrafiltration treatment on the filtrate obtained in the step e to remove residual suspended matters and colloid in the filtrate to obtain ultrafiltration water;
step g: performing reverse osmosis treatment on the ultrafiltration produced water in the step f to obtain reverse osmosis concentrated water and reverse osmosis produced water;
step h: performing electrodialysis treatment on the reverse osmosis concentrated water obtained in the step g to obtain electrodialysis concentrated solution and electrodialysis fresh water, and performing evaporation crystallization treatment on the electrodialysis concentrated solution to obtain crystallized salt and reuse water;
step i: drying the residual mother liquor in the step h by using a spray dryer to obtain mixed salt, and transporting the generated mixed salt out for safe landfill;
step j: and c, storing the sodium sulfate crystals and the sodium nitrate crystals obtained in the step c and the step d in special storage bottles.
Preferably, the concentrated brine in step a contains organic pollutants including phenols, polycyclic aromatic compounds, heterocyclic compounds containing nitrogen, oxygen and sulfur, and the like, the dichromate index is generally about 4000mg/L to 5000mg/L, the ammonia nitrogen content is 200mg/L to 500mg/L, the salt content in the wastewater is high, and the TDS is generally 500mg/L to 5000 mg/L.
Preferably, the treatment method in the step b, the step c and the step d further comprises drying the obtained sodium sulfate crystals, sodium chloride crystals and sodium nitrate crystals, wherein a heat source of the drying treatment is low-pressure saturated steam with the temperature of less than 150 ℃.
Preferably, the sodium sulfate crystallization unit of step c includes a sodium sulfate crystallization tank for performing sodium sulfate crystallization on the high-concentration brine to obtain a sodium sulfate slurry and a mother liquor, a first thickener for performing thickening and crystal growth treatment on the sodium sulfate slurry, and a first centrifuge for centrifuging the thickened sodium sulfate slurry.
Preferably, the sodium chloride crystallization unit of step e includes a sodium chloride crystallization tank for performing sodium chloride crystallization on the mother liquor obtained through sodium sulfate crystallization to obtain a sodium chloride slurry and the mother liquor, a second thickener for performing thickening and crystal growth on the sodium chloride slurry, and a second centrifuge for centrifugally separating the thickened sodium chloride slurry.
Preferably, the purity of the industrial sodium chloride crystal obtained by the step e crystallization is more than 90%.
Preferably, the treatment equipment of step c, step e and step d further comprises a drying unit for drying crystals obtained from the sodium sulfate crystallization unit, the sodium chloride crystallization unit and the sodium nitrate crystallization unit respectively.
Compared with the prior art, the invention has the following beneficial effects:
the invention realizes zero discharge of high-concentration brine by sodium chloride and sodium sulfate separated from the high-concentration brine of coal-to-liquids, well ensures the purity of the sodium chloride and the sodium sulfate, respectively crystallizes the sodium chloride, the sodium sulfate and the sodium nitrate in the high-concentration brine to reach industrial products, finally realizes the process technology of resource utilization of crystallized salt and zero discharge of wastewater, and solves the problem of non-ideal wastewater zero discharge of coal chemical industry enterprises in chemical treatment.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
The treatment process and method of the crystallization salt of the high-concentration salt aquatic product of the coal-to-liquid comprises the following steps:
step a: firstly, passing strong brine through an activated carbon adsorption tower, and reducing the concentration of the high strong brine of the coal-to-liquid fuel through activated carbon adsorption;
step b: b, adding sodium hydroxide into the coal-to-liquids high-concentration brine with the concentration reduced in the step a to enable pollution factors to form precipitates, adding sodium carbonate, stirring to enable the sodium hydroxide to fully react in the coal-to-liquids high-concentration brine, forming calcium carbonate precipitates with the remaining calcium ions, standing, and taking supernatant to obtain clear liquor;
step c: b, sequentially carrying out preheating treatment and evaporative concentration treatment on the clarified liquid obtained in the step b, carrying out sodium sulfate crystallization treatment on the high-concentration brine subjected to evaporative concentration treatment to obtain sodium sulfate slurry and mother liquor, carrying out thickening and crystal growth treatment on the sodium sulfate slurry, and then carrying out centrifugal separation to obtain sodium sulfate crystals, wherein the clarified liquid is subjected to sodium sulfate crystallization treatment through cooling and cooling;
step d: c, crystallizing the mother liquor obtained in the step c to obtain sodium nitrate slurry and the mother liquor, and centrifugally separating the sodium nitrate slurry to obtain sodium nitrate crystals;
step e: d, carrying out sodium chloride crystallization treatment on the mother liquor obtained in the step d to obtain sodium chloride slurry and the mother liquor, and carrying out thickening and crystal growth treatment on the obtained sodium chloride slurry and then carrying out centrifugal separation to obtain sodium chloride crystals;
step f: e, performing ultrafiltration treatment on the filtrate obtained in the step e to remove residual suspended matters and colloid in the filtrate to obtain ultrafiltration water;
step g: performing reverse osmosis treatment on the ultrafiltration produced water in the step f to obtain reverse osmosis concentrated water and reverse osmosis produced water;
step h: performing electrodialysis treatment on the reverse osmosis concentrated water obtained in the step g to obtain electrodialysis concentrated solution and electrodialysis fresh water, and performing evaporation crystallization treatment on the electrodialysis concentrated solution to obtain crystallized salt and reuse water;
step i: drying the residual mother liquor in the step h by using a spray dryer to obtain mixed salt, and transporting the generated mixed salt out for safe landfill;
step j: and c, storing the sodium sulfate crystals and the sodium nitrate crystals obtained in the step c and the step d in special storage bottles.
Example 1
The treatment process and method of the crystallization salt of the high-concentration salt aquatic product of the coal-to-liquid comprises the following steps:
step a: firstly, passing strong brine through an activated carbon adsorption tower, and reducing the concentration of the high strong brine of the coal-to-liquid fuel through activated carbon adsorption;
step b: b, adding sodium hydroxide into the coal-to-liquids high-concentration brine with the concentration reduced in the step a to enable pollution factors to form precipitates, adding sodium carbonate, stirring to enable the sodium hydroxide to fully react in the coal-to-liquids high-concentration brine, forming calcium carbonate precipitates with the remaining calcium ions, standing, and taking supernatant to obtain clear liquor;
step c: b, sequentially carrying out preheating treatment and evaporative concentration treatment on the clarified liquid obtained in the step b, carrying out sodium sulfate crystallization treatment on the high-concentration brine subjected to evaporative concentration treatment to obtain sodium sulfate slurry and mother liquor, carrying out thickening and crystal growth treatment on the sodium sulfate slurry, and then carrying out centrifugal separation to obtain sodium sulfate crystals, wherein the clarified liquid is subjected to sodium sulfate crystallization treatment through cooling and cooling;
step d: c, crystallizing the mother liquor obtained in the step c to obtain sodium nitrate slurry and the mother liquor, and centrifugally separating the sodium nitrate slurry to obtain sodium nitrate crystals;
step e: d, carrying out sodium chloride crystallization treatment on the mother liquor obtained in the step d to obtain sodium chloride slurry and the mother liquor, and carrying out thickening and crystal growth treatment on the obtained sodium chloride slurry and then carrying out centrifugal separation to obtain sodium chloride crystals;
step f: e, performing ultrafiltration treatment on the filtrate obtained in the step e to remove residual suspended matters and colloid in the filtrate to obtain ultrafiltration water;
step g: performing reverse osmosis treatment on the ultrafiltration produced water in the step f to obtain reverse osmosis concentrated water and reverse osmosis produced water;
step h: performing electrodialysis treatment on the reverse osmosis concentrated water obtained in the step g to obtain electrodialysis concentrated solution and electrodialysis fresh water, and performing evaporation crystallization treatment on the electrodialysis concentrated solution to obtain crystallized salt and reuse water;
step i: drying the residual mother liquor in the step h by using a spray dryer to obtain mixed salt, and transporting the generated mixed salt out for safe landfill;
step j: and c, storing the sodium sulfate crystals and the sodium nitrate crystals obtained in the step c and the step d in special storage bottles.
Example 2
In example 1, the following additional steps were added:
in the step a, the concentrated brine contains organic pollutants including phenols, polycyclic aromatic compounds, heterocyclic compounds containing nitrogen, oxygen and sulfur and the like, the dichromate index is about 4000 mg/L-5000 mg/L generally, the ammonia nitrogen content is 200 mg/L-500 mg/L, the salt content in the wastewater is high, and the TDS is 500 mg/L-5000 mg/L generally.
The treatment process and method of the crystallization salt of the high-concentration salt aquatic product of the coal-to-liquid comprises the following steps:
step a: firstly, passing strong brine through an activated carbon adsorption tower, and reducing the concentration of the high strong brine of the coal-to-liquid fuel through activated carbon adsorption;
step b: b, adding sodium hydroxide into the coal-to-liquids high-concentration brine with the concentration reduced in the step a to enable pollution factors to form precipitates, adding sodium carbonate, stirring to enable the sodium hydroxide to fully react in the coal-to-liquids high-concentration brine, forming calcium carbonate precipitates with the remaining calcium ions, standing, and taking supernatant to obtain clear liquor;
step c: b, sequentially carrying out preheating treatment and evaporative concentration treatment on the clarified liquid obtained in the step b, carrying out sodium sulfate crystallization treatment on the high-concentration brine subjected to evaporative concentration treatment to obtain sodium sulfate slurry and mother liquor, carrying out thickening and crystal growth treatment on the sodium sulfate slurry, and then carrying out centrifugal separation to obtain sodium sulfate crystals, wherein the clarified liquid is subjected to sodium sulfate crystallization treatment through cooling and cooling;
step d: c, crystallizing the mother liquor obtained in the step c to obtain sodium nitrate slurry and the mother liquor, and centrifugally separating the sodium nitrate slurry to obtain sodium nitrate crystals;
step e: d, carrying out sodium chloride crystallization treatment on the mother liquor obtained in the step d to obtain sodium chloride slurry and the mother liquor, and carrying out thickening and crystal growth treatment on the obtained sodium chloride slurry and then carrying out centrifugal separation to obtain sodium chloride crystals;
step f: e, performing ultrafiltration treatment on the filtrate obtained in the step e to remove residual suspended matters and colloid in the filtrate to obtain ultrafiltration water;
step g: performing reverse osmosis treatment on the ultrafiltration produced water in the step f to obtain reverse osmosis concentrated water and reverse osmosis produced water;
step h: performing electrodialysis treatment on the reverse osmosis concentrated water obtained in the step g to obtain electrodialysis concentrated solution and electrodialysis fresh water, and performing evaporation crystallization treatment on the electrodialysis concentrated solution to obtain crystallized salt and reuse water;
step i: drying the residual mother liquor in the step h by using a spray dryer to obtain mixed salt, and transporting the generated mixed salt out for safe landfill;
step j: and c, storing the sodium sulfate crystals and the sodium nitrate crystals obtained in the step c and the step d in special storage bottles.
Example 3
In example 2, the following steps were added:
the treatment method in the step b, the step c and the step d further comprises the step of drying the obtained sodium sulfate crystals, sodium chloride crystals and sodium nitrate crystals, wherein the heat source of the drying treatment is low-pressure saturated steam with the temperature of less than 150 ℃.
The treatment process and method of the crystallization salt of the high-concentration salt aquatic product of the coal-to-liquid comprises the following steps:
step a: firstly, passing strong brine through an activated carbon adsorption tower, and reducing the concentration of the high strong brine of the coal-to-liquid fuel through activated carbon adsorption;
step b: b, adding sodium hydroxide into the coal-to-liquids high-concentration brine with the concentration reduced in the step a to enable pollution factors to form precipitates, adding sodium carbonate, stirring to enable the sodium hydroxide to fully react in the coal-to-liquids high-concentration brine, forming calcium carbonate precipitates with the remaining calcium ions, standing, and taking supernatant to obtain clear liquor;
step c: b, sequentially carrying out preheating treatment and evaporative concentration treatment on the clarified liquid obtained in the step b, carrying out sodium sulfate crystallization treatment on the high-concentration brine subjected to evaporative concentration treatment to obtain sodium sulfate slurry and mother liquor, carrying out thickening and crystal growth treatment on the sodium sulfate slurry, and then carrying out centrifugal separation to obtain sodium sulfate crystals, wherein the clarified liquid is subjected to sodium sulfate crystallization treatment through cooling and cooling;
step d: c, crystallizing the mother liquor obtained in the step c to obtain sodium nitrate slurry and the mother liquor, and centrifugally separating the sodium nitrate slurry to obtain sodium nitrate crystals;
step e: d, carrying out sodium chloride crystallization treatment on the mother liquor obtained in the step d to obtain sodium chloride slurry and the mother liquor, and carrying out thickening and crystal growth treatment on the obtained sodium chloride slurry and then carrying out centrifugal separation to obtain sodium chloride crystals;
step f: e, performing ultrafiltration treatment on the filtrate obtained in the step e to remove residual suspended matters and colloid in the filtrate to obtain ultrafiltration water;
step g: performing reverse osmosis treatment on the ultrafiltration produced water in the step f to obtain reverse osmosis concentrated water and reverse osmosis produced water;
step h: performing electrodialysis treatment on the reverse osmosis concentrated water obtained in the step g to obtain electrodialysis concentrated solution and electrodialysis fresh water, and performing evaporation crystallization treatment on the electrodialysis concentrated solution to obtain crystallized salt and reuse water;
step i: drying the residual mother liquor in the step h by using a spray dryer to obtain mixed salt, and transporting the generated mixed salt out for safe landfill;
step j: and c, storing the sodium sulfate crystals and the sodium nitrate crystals obtained in the step c and the step d in special storage bottles.
Example 4
In example 3, the following steps were added:
the sodium sulfate crystallization unit of step c includes a sodium sulfate crystallization tank for performing sodium sulfate crystallization treatment on the high-concentration brine to obtain a sodium sulfate slurry and a mother liquor, a first thickener for performing thickening and crystal growth treatment on the sodium sulfate slurry, and a first centrifuge for centrifuging the thickened sodium sulfate slurry.
The treatment process and method of the crystallization salt of the high-concentration salt aquatic product of the coal-to-liquid comprises the following steps:
step a: firstly, passing strong brine through an activated carbon adsorption tower, and reducing the concentration of the high strong brine of the coal-to-liquid fuel through activated carbon adsorption;
step b: b, adding sodium hydroxide into the coal-to-liquids high-concentration brine with the concentration reduced in the step a to enable pollution factors to form precipitates, adding sodium carbonate, stirring to enable the sodium hydroxide to fully react in the coal-to-liquids high-concentration brine, forming calcium carbonate precipitates with the remaining calcium ions, standing, and taking supernatant to obtain clear liquor;
step c: b, sequentially carrying out preheating treatment and evaporative concentration treatment on the clarified liquid obtained in the step b, carrying out sodium sulfate crystallization treatment on the high-concentration brine subjected to evaporative concentration treatment to obtain sodium sulfate slurry and mother liquor, carrying out thickening and crystal growth treatment on the sodium sulfate slurry, and then carrying out centrifugal separation to obtain sodium sulfate crystals, wherein the clarified liquid is subjected to sodium sulfate crystallization treatment through cooling and cooling;
step d: c, crystallizing the mother liquor obtained in the step c to obtain sodium nitrate slurry and the mother liquor, and centrifugally separating the sodium nitrate slurry to obtain sodium nitrate crystals;
step e: d, carrying out sodium chloride crystallization treatment on the mother liquor obtained in the step d to obtain sodium chloride slurry and the mother liquor, and carrying out thickening and crystal growth treatment on the obtained sodium chloride slurry and then carrying out centrifugal separation to obtain sodium chloride crystals;
step f: e, performing ultrafiltration treatment on the filtrate obtained in the step e to remove residual suspended matters and colloid in the filtrate to obtain ultrafiltration water;
step g: performing reverse osmosis treatment on the ultrafiltration produced water in the step f to obtain reverse osmosis concentrated water and reverse osmosis produced water;
step h: performing electrodialysis treatment on the reverse osmosis concentrated water obtained in the step g to obtain electrodialysis concentrated solution and electrodialysis fresh water, and performing evaporation crystallization treatment on the electrodialysis concentrated solution to obtain crystallized salt and reuse water;
step i: drying the residual mother liquor in the step h by using a spray dryer to obtain mixed salt, and transporting the generated mixed salt out for safe landfill;
step j: and c, storing the sodium sulfate crystals and the sodium nitrate crystals obtained in the step c and the step d in special storage bottles.
Example 5
In example 4, the following steps were added:
the sodium chloride crystallization unit in the step e comprises a sodium chloride crystallization tank for performing sodium chloride crystallization treatment on the mother liquor obtained through sodium sulfate crystallization treatment to obtain sodium chloride slurry and the mother liquor, a second thickener for performing thickening and crystal growth treatment on the sodium chloride slurry, and a second centrifuge for performing centrifugal separation on the thickened sodium chloride slurry.
The treatment process and method of the crystallization salt of the high-concentration salt aquatic product of the coal-to-liquid comprises the following steps:
step a: firstly, passing strong brine through an activated carbon adsorption tower, and reducing the concentration of the high strong brine of the coal-to-liquid fuel through activated carbon adsorption;
step b: b, adding sodium hydroxide into the coal-to-liquids high-concentration brine with the concentration reduced in the step a to enable pollution factors to form precipitates, adding sodium carbonate, stirring to enable the sodium hydroxide to fully react in the coal-to-liquids high-concentration brine, forming calcium carbonate precipitates with the remaining calcium ions, standing, and taking supernatant to obtain clear liquor;
step c: b, sequentially carrying out preheating treatment and evaporative concentration treatment on the clarified liquid obtained in the step b, carrying out sodium sulfate crystallization treatment on the high-concentration brine subjected to evaporative concentration treatment to obtain sodium sulfate slurry and mother liquor, carrying out thickening and crystal growth treatment on the sodium sulfate slurry, and then carrying out centrifugal separation to obtain sodium sulfate crystals, wherein the clarified liquid is subjected to sodium sulfate crystallization treatment through cooling and cooling;
step d: c, crystallizing the mother liquor obtained in the step c to obtain sodium nitrate slurry and the mother liquor, and centrifugally separating the sodium nitrate slurry to obtain sodium nitrate crystals;
step e: d, carrying out sodium chloride crystallization treatment on the mother liquor obtained in the step d to obtain sodium chloride slurry and the mother liquor, and carrying out thickening and crystal growth treatment on the obtained sodium chloride slurry and then carrying out centrifugal separation to obtain sodium chloride crystals;
step f: e, performing ultrafiltration treatment on the filtrate obtained in the step e to remove residual suspended matters and colloid in the filtrate to obtain ultrafiltration water;
step g: performing reverse osmosis treatment on the ultrafiltration produced water in the step f to obtain reverse osmosis concentrated water and reverse osmosis produced water;
step h: performing electrodialysis treatment on the reverse osmosis concentrated water obtained in the step g to obtain electrodialysis concentrated solution and electrodialysis fresh water, and performing evaporation crystallization treatment on the electrodialysis concentrated solution to obtain crystallized salt and reuse water;
step i: drying the residual mother liquor in the step h by using a spray dryer to obtain mixed salt, and transporting the generated mixed salt out for safe landfill;
step j: and c, storing the sodium sulfate crystals and the sodium nitrate crystals obtained in the step c and the step d in special storage bottles.
Example 6
In example 5, the following steps were added:
and e, crystallizing to obtain the industrial sodium chloride crystal with the purity of more than 90%.
The treatment process and method of the crystallization salt of the high-concentration salt aquatic product of the coal-to-liquid comprises the following steps:
step a: firstly, passing strong brine through an activated carbon adsorption tower, and reducing the concentration of the high strong brine of the coal-to-liquid fuel through activated carbon adsorption;
step b: b, adding sodium hydroxide into the coal-to-liquids high-concentration brine with the concentration reduced in the step a to enable pollution factors to form precipitates, adding sodium carbonate, stirring to enable the sodium hydroxide to fully react in the coal-to-liquids high-concentration brine, forming calcium carbonate precipitates with the remaining calcium ions, standing, and taking supernatant to obtain clear liquor;
step c: b, sequentially carrying out preheating treatment and evaporative concentration treatment on the clarified liquid obtained in the step b, carrying out sodium sulfate crystallization treatment on the high-concentration brine subjected to evaporative concentration treatment to obtain sodium sulfate slurry and mother liquor, carrying out thickening and crystal growth treatment on the sodium sulfate slurry, and then carrying out centrifugal separation to obtain sodium sulfate crystals, wherein the clarified liquid is subjected to sodium sulfate crystallization treatment through cooling and cooling;
step d: c, crystallizing the mother liquor obtained in the step c to obtain sodium nitrate slurry and the mother liquor, and centrifugally separating the sodium nitrate slurry to obtain sodium nitrate crystals;
step e: d, carrying out sodium chloride crystallization treatment on the mother liquor obtained in the step d to obtain sodium chloride slurry and the mother liquor, and carrying out thickening and crystal growth treatment on the obtained sodium chloride slurry and then carrying out centrifugal separation to obtain sodium chloride crystals;
step f: e, performing ultrafiltration treatment on the filtrate obtained in the step e to remove residual suspended matters and colloid in the filtrate to obtain ultrafiltration water;
step g: performing reverse osmosis treatment on the ultrafiltration produced water in the step f to obtain reverse osmosis concentrated water and reverse osmosis produced water;
step h: performing electrodialysis treatment on the reverse osmosis concentrated water obtained in the step g to obtain electrodialysis concentrated solution and electrodialysis fresh water, and performing evaporation crystallization treatment on the electrodialysis concentrated solution to obtain crystallized salt and reuse water;
step i: drying the residual mother liquor in the step h by using a spray dryer to obtain mixed salt, and transporting the generated mixed salt out for safe landfill;
step j: and c, storing the sodium sulfate crystals and the sodium nitrate crystals obtained in the step c and the step d in special storage bottles.
Although embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that changes, modifications, substitutions and alterations can be made in these embodiments without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents.
Claims (7)
1. The treatment process and the method for the high-concentration salt aquatic product crystallization salt of the coal-to-liquid are characterized by comprising the following steps of: the method comprises the following steps:
step a: firstly, passing strong brine through an activated carbon adsorption tower, and reducing the concentration of the high strong brine of the coal-to-liquid fuel through activated carbon adsorption;
step b: b, adding sodium hydroxide into the coal-to-liquids high-concentration brine with the concentration reduced in the step a to enable pollution factors to form precipitates, adding sodium carbonate, stirring to enable the sodium hydroxide to fully react in the coal-to-liquids high-concentration brine, forming calcium carbonate precipitates with the remaining calcium ions, standing, and taking supernatant to obtain clear liquor;
step c: b, sequentially carrying out preheating treatment and evaporation concentration treatment on the clarified liquid obtained in the step b, carrying out sodium sulfate crystallization treatment on high-concentration brine subjected to evaporation concentration treatment to obtain sodium sulfate slurry and mother liquor, carrying out thickening and crystal growth treatment on the sodium sulfate slurry, and then carrying out centrifugal separation to obtain sodium sulfate crystals, wherein the clarified liquid is subjected to sodium sulfate crystallization treatment through cooling and temperature reduction;
step d: c, crystallizing the mother liquor obtained in the step c to obtain sodium nitrate slurry and the mother liquor, and centrifugally separating the sodium nitrate slurry to obtain sodium nitrate crystals;
step e: d, carrying out sodium chloride crystallization treatment on the mother liquor obtained in the step d to obtain sodium chloride slurry and the mother liquor, and carrying out thickening and crystal growth treatment on the obtained sodium chloride slurry and then carrying out centrifugal separation to obtain sodium chloride crystals;
step f: e, performing ultrafiltration treatment on the filtrate obtained in the step e to remove residual suspended matters and colloid in the filtrate to obtain ultrafiltration water;
step g: performing reverse osmosis treatment on the ultrafiltration produced water in the step f to obtain reverse osmosis concentrated water and reverse osmosis produced water;
step h: performing electrodialysis treatment on the reverse osmosis concentrated water obtained in the step g to obtain electrodialysis concentrated solution and electrodialysis fresh water, and performing evaporation crystallization treatment on the electrodialysis concentrated solution to obtain crystallized salt and reuse water;
step i: drying the residual mother liquor in the step h by using a spray dryer to obtain mixed salt, and transporting the generated mixed salt out for safe landfill;
step j: and c, storing the sodium sulfate crystals and the sodium nitrate crystals obtained in the step c and the step d in special storage bottles.
2. The coal-to-liquids high concentrated salt aquatic product crystallization salt treatment process and method according to claim 1 are characterized in that: in the step a, the concentrated brine contains organic pollutants including phenols, polycyclic aromatic compounds, heterocyclic compounds containing nitrogen, oxygen and sulfur and the like, the dichromate index is about 4000 mg/L-5000 mg/L generally, the ammonia nitrogen content is 200 mg/L-500 mg/L, the salt content in the wastewater is high, and the TDS is 500 mg/L-5000 mg/L generally.
3. The coal-to-liquids high concentrated salt aquatic product crystallization salt treatment process and method according to claim 1 are characterized in that: the treatment method in the step b, the step c and the step d further comprises the step of drying the obtained sodium sulfate crystals, sodium chloride crystals and sodium nitrate crystals, wherein a heat source of the drying treatment is low-pressure saturated steam with the temperature of less than 150 ℃.
4. The coal-to-liquids high concentrated salt aquatic product crystallization salt treatment process and method according to claim 1 are characterized in that: the sodium sulfate crystallization unit of the step c comprises a sodium sulfate crystallization tank for performing sodium sulfate crystallization treatment on the high-concentration brine to obtain sodium sulfate slurry and mother liquor, a first thickener for performing thickening and crystal growth treatment on the sodium sulfate slurry, and a first centrifuge for performing centrifugal separation on the thickened sodium sulfate slurry.
5. The coal-to-liquids high concentrated salt aquatic product crystallization salt treatment process and method according to claim 1 are characterized in that: and the sodium chloride crystallization unit in the step e comprises a sodium chloride crystallization tank for performing sodium chloride crystallization treatment on the mother liquor obtained through sodium sulfate crystallization treatment to obtain sodium chloride slurry and the mother liquor, a second thickener for performing thickening and crystal growth treatment on the sodium chloride slurry, and a second centrifuge for performing centrifugal separation on the thickened sodium chloride slurry.
6. The coal-to-liquids high concentrated salt aquatic product crystallization salt treatment process and method according to claim 1 are characterized in that: the purity of the industrial sodium chloride crystal obtained by crystallization in the step e is more than 90%.
7. The coal-to-liquids high concentrated salt aquatic product crystallization salt treatment process and method according to claim 1 are characterized in that: the treatment equipment in the steps c, e and d further comprises a drying unit for drying crystals obtained by the sodium sulfate crystallization unit, the sodium chloride crystallization unit and the sodium nitrate crystallization unit respectively.
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20030080066A1 (en) * | 2001-10-29 | 2003-05-01 | Vohra Rajinder N. | Recovery of common salt and marine chemicals from brine |
| CN105502438A (en) * | 2015-12-17 | 2016-04-20 | 深圳能源资源综合开发有限公司 | Treatment method and device for coal chemical industry high-concentration brine |
| CN105948362A (en) * | 2016-06-24 | 2016-09-21 | 东华工程科技股份有限公司 | Coal chemical RO strong brine treatment process |
| WO2017181696A1 (en) * | 2016-04-21 | 2017-10-26 | 广州市心德实业有限公司 | Method for treating and recycling brine wastewater containing sodium chloride and sodium sulfate |
| CN107840511A (en) * | 2017-11-10 | 2018-03-27 | 深圳能源资源综合开发有限公司 | Coal chemical industry method for treating strong brine and system |
-
2021
- 2021-12-29 CN CN202111639853.6A patent/CN114368867A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20030080066A1 (en) * | 2001-10-29 | 2003-05-01 | Vohra Rajinder N. | Recovery of common salt and marine chemicals from brine |
| CN105502438A (en) * | 2015-12-17 | 2016-04-20 | 深圳能源资源综合开发有限公司 | Treatment method and device for coal chemical industry high-concentration brine |
| WO2017181696A1 (en) * | 2016-04-21 | 2017-10-26 | 广州市心德实业有限公司 | Method for treating and recycling brine wastewater containing sodium chloride and sodium sulfate |
| CN105948362A (en) * | 2016-06-24 | 2016-09-21 | 东华工程科技股份有限公司 | Coal chemical RO strong brine treatment process |
| CN107840511A (en) * | 2017-11-10 | 2018-03-27 | 深圳能源资源综合开发有限公司 | Coal chemical industry method for treating strong brine and system |
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