CN215391554U - Waste salt resourceful treatment system - Google Patents
Waste salt resourceful treatment system Download PDFInfo
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- CN215391554U CN215391554U CN202121925274.3U CN202121925274U CN215391554U CN 215391554 U CN215391554 U CN 215391554U CN 202121925274 U CN202121925274 U CN 202121925274U CN 215391554 U CN215391554 U CN 215391554U
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- 150000003839 salts Chemical class 0.000 title claims abstract description 76
- 239000002699 waste material Substances 0.000 title claims abstract description 41
- 238000000197 pyrolysis Methods 0.000 claims abstract description 71
- 239000010802 sludge Substances 0.000 claims abstract description 24
- 238000002425 crystallisation Methods 0.000 claims abstract description 23
- 230000008025 crystallization Effects 0.000 claims abstract description 23
- 238000004064 recycling Methods 0.000 claims abstract description 20
- 238000004062 sedimentation Methods 0.000 claims abstract description 20
- 238000001914 filtration Methods 0.000 claims abstract description 17
- 238000003763 carbonization Methods 0.000 claims abstract description 16
- 239000007788 liquid Substances 0.000 claims abstract description 11
- 238000000926 separation method Methods 0.000 claims abstract description 10
- 239000012267 brine Substances 0.000 claims abstract description 7
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims abstract description 7
- 239000003814 drug Substances 0.000 claims abstract description 6
- 238000007670 refining Methods 0.000 claims abstract description 6
- 238000011084 recovery Methods 0.000 claims abstract description 5
- 238000003756 stirring Methods 0.000 claims abstract description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 25
- 230000000694 effects Effects 0.000 claims description 18
- 238000001728 nano-filtration Methods 0.000 claims description 17
- 239000012452 mother liquor Substances 0.000 claims description 13
- 239000007789 gas Substances 0.000 claims description 12
- 238000001704 evaporation Methods 0.000 claims description 11
- 230000008020 evaporation Effects 0.000 claims description 10
- 238000010438 heat treatment Methods 0.000 claims description 9
- 239000002002 slurry Substances 0.000 claims description 9
- 238000000108 ultra-filtration Methods 0.000 claims description 9
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 6
- 238000000746 purification Methods 0.000 claims description 6
- 229920001429 chelating resin Polymers 0.000 claims description 3
- 238000005485 electric heating Methods 0.000 claims description 3
- 238000004519 manufacturing process Methods 0.000 claims description 3
- 239000003345 natural gas Substances 0.000 claims description 3
- 239000012266 salt solution Substances 0.000 claims 1
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 abstract description 22
- 239000011780 sodium chloride Substances 0.000 abstract description 13
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 abstract description 11
- 150000002500 ions Chemical class 0.000 abstract description 10
- 229910052938 sodium sulfate Inorganic materials 0.000 abstract description 9
- 235000011152 sodium sulphate Nutrition 0.000 abstract description 9
- 238000000034 method Methods 0.000 description 6
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 5
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 4
- 238000002485 combustion reaction Methods 0.000 description 4
- 239000003546 flue gas Substances 0.000 description 4
- 229910052760 oxygen Inorganic materials 0.000 description 4
- 239000001301 oxygen Substances 0.000 description 4
- 238000005406 washing Methods 0.000 description 4
- 238000009875 water degumming Methods 0.000 description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 239000000428 dust Substances 0.000 description 3
- 229910017053 inorganic salt Inorganic materials 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 239000002918 waste heat Substances 0.000 description 3
- ODINCKMPIJJUCX-UHFFFAOYSA-N Calcium oxide Chemical compound [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 239000002920 hazardous waste Substances 0.000 description 2
- 229910001385 heavy metal Inorganic materials 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 239000000575 pesticide Substances 0.000 description 2
- 238000010791 quenching Methods 0.000 description 2
- 239000002893 slag Substances 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 230000032683 aging Effects 0.000 description 1
- 238000011001 backwashing Methods 0.000 description 1
- 239000000292 calcium oxide Substances 0.000 description 1
- 235000012255 calcium oxide Nutrition 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 239000000706 filtrate Substances 0.000 description 1
- 150000004820 halides Chemical class 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- -1 partial alkalinity Inorganic materials 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 230000000171 quenching effect Effects 0.000 description 1
- 229910052710 silicon Inorganic materials 0.000 description 1
- 239000010703 silicon Substances 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
- 239000012855 volatile organic compound Substances 0.000 description 1
- 230000002087 whitening effect Effects 0.000 description 1
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- Separation Using Semi-Permeable Membranes (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Abstract
The utility model discloses a waste salt recycling treatment system, which comprises a carbonization pyrolysis unit, a brine refining unit and a salt separation crystallization unit which are sequentially connected; the brine refining unit comprises a salt dissolving tank, a high-efficiency sedimentation tank, a filtering device, a COD removing device and an ion exchanger which are sequentially connected; the efficient sedimentation tank is provided with a medicament feeding port and a stirring device, the efficient sedimentation tank and the filtering device are both connected with a sludge dewatering device, and the sludge dewatering device is also connected with a sludge recovery tank; the sludge dewatering device is also provided with a liquid outlet, and the liquid outlet is connected with the high-efficiency sedimentation tank through a return pipe. According to the waste salt recycling treatment system provided by the utility model, the waste salt is refined, the removal rate of organic matters can reach more than 60% through carbonization and pyrolysis, and meanwhile, product-grade sodium chloride and sodium sulfate are recovered.
Description
Technical Field
The utility model belongs to the technical field of waste salt treatment, and particularly relates to a waste salt recycling treatment system.
Background
In industrial production processes, particularly in coal chemical industry, chemical fertilizers, pesticides, biochemical industry and the like, industrial salt residues such as distillation residues (HW 11) in non-specific industries, pesticide industry (HW 04), pharmaceutical industry (HW02), organic halide-containing waste (HW 45) and the like often generate a large amount of solid waste salt, and the main components are sodium chloride and sodium sulfate. These waste salts often contain a certain amount of organic or heavy metals and other impurities, and are also classified as hazardous waste by the state-related legal documents. Waste salt is generally stored temporarily in a centralized manner in a warehouse building manner in the prior art, but how to thoroughly realize harmless recycling becomes an industrial problem to be solved urgently.
The existing waste salt treatment technology mainly comprises landfill, incineration and resource comprehensive utilization. The landfill is to carry out sanitary landfill disposal by curing waste salt through concrete and the like and then sending the waste salt into a rigid landfill site according to landfill technical specifications. The incineration is that the waste salt is heated to 900 ℃, the inorganic salt is melted and flows into the furnace bottom, and the inorganic salt is cooled and recovered. Because the melting point interval of the waste salt has large fluctuation, adverse phenomena such as slag bonding, caking and the like are easy to occur in the incineration treatment process, and the process stability is influenced.
The hazardous waste salt has high yield and high environmental hazard, has very high recycling value, treats the waste salt, realizes the recycling of the waste salt, can solve the problem of environmental pollution and bring considerable benefits.
SUMMERY OF THE UTILITY MODEL
Aiming at the defects of the prior art, the utility model provides a waste salt recycling treatment system which can effectively remove organic matters in waste salt and simultaneously recover sodium chloride and sodium sulfate in the waste salt.
A waste salt recycling treatment system comprises a carbonization pyrolysis unit, a salt water refining unit and a salt separation crystallization unit which are sequentially connected, wherein the salt water refining unit comprises a salt dissolving tank, a high-efficiency sedimentation tank, a filtering device, a COD removing device and an ion exchanger which are sequentially connected; the efficient sedimentation tank is provided with a medicament feeding port and a stirring device, the efficient sedimentation tank and the filtering device are both connected with a sludge dewatering device, and the sludge dewatering device is also connected with a sludge recovery tank; the sludge dewatering device is also provided with a liquid outlet, and the liquid outlet is connected with the high-efficiency sedimentation tank through a return pipe.
Preferably, the salt separation crystallization unit comprises a nanofiltration device, an evaporation crystallization device and a mother liquor tank which are connected in sequence;
the evaporative crystallization device is also connected with a salt dissolving tank; the mother liquor tank is connected with the carbonization pyrolysis unit; the inlet of the nanofiltration device is connected with the ion exchanger;
the evaporative crystallization device is a four-effect evaporative crystallizer; the four-effect evaporation crystallizer comprises a first effect evaporator, a second effect evaporator, a third effect evaporator and a fourth effect evaporator which are sequentially connected; refined salt slurry outlets are formed in the bottoms of the second effect evaporator and the fourth effect evaporator;
and a water production outlet and a concentrated water outlet of the nanofiltration device are respectively connected with feed inlets of the third effect evaporator and the first effect evaporator.
Preferably, the carbonization pyrolysis unit comprises a primary pyrolysis device and a secondary pyrolysis device which are connected in sequence, and the primary pyrolysis device and the secondary pyrolysis device are both connected with the tail gas purification unit; the secondary pyrolysis device is connected with the salt dissolving tank; the primary pyrolysis device is connected with a mother liquor tank.
Preferably, the primary pyrolysis device and the secondary pyrolysis device are both fixed beds or fluidized beds.
Preferably, the fixed bed is a rotary kiln or a rake furnace.
Preferably, the heating modes of the primary pyrolysis device and the secondary pyrolysis device are electric heating, natural gas heating or microwave heating.
Preferably, the carbonization pyrolysis unit further comprises a first crushing device and a second crushing device, the first crushing device is connected with an inlet of the first-stage pyrolysis device, and the first-stage pyrolysis device and the second-stage pyrolysis device are connected through the second crushing device.
Preferably, the filtering device is formed by connecting a multi-medium filtering device and an ultrafiltration device, or is one of a tubular ultrafiltration device and an immersed ultrafiltration device.
Preferably, the sludge dewatering device is a filter press.
Preferably, the ion exchanger is a chelating resin ion exchanger.
The utility model has the advantages that:
according to the waste salt recycling treatment system provided by the utility model, the waste salt is refined, the removal rate of organic matters can reach more than 60% through carbonization and pyrolysis, and meanwhile, product-grade sodium chloride and sodium sulfate are recovered.
Drawings
FIG. 1 is a schematic view of the structural connection of a waste salt recycling system;
FIG. 2 is a schematic diagram of the connection of a nanofiltration device and an evaporative crystallization device;
the device comprises a first-effect evaporator, a second-effect evaporator, a third-effect evaporator, a fourth-effect evaporator and a nanofiltration device, wherein the first-effect evaporator is 1, the second-effect evaporator is 2, the third-effect evaporator is 3, the fourth-effect evaporator is 4, and the nanofiltration device is 5.
Detailed Description
The utility model is further described below with reference to the accompanying drawings.
Example 1
A waste salt recycling treatment system comprises a carbonization pyrolysis unit, a salt water refining unit and a salt separation crystallization unit which are sequentially connected, wherein the salt water refining unit comprises a salt dissolving tank, a high-efficiency sedimentation tank, a filtering device, a COD removing device and an ion exchanger which are sequentially connected; the efficient sedimentation tank is provided with a medicament feeding port and a stirring device, the efficient sedimentation tank and the filtering device are both connected with a sludge dewatering device, and the sludge dewatering device is also connected with a sludge recovery tank; the sludge dewatering device is also provided with a liquid outlet, and the liquid outlet is connected with the high-efficiency sedimentation tank through a return pipe.
Example 2
On the basis of the embodiment 1, the salt separation crystallization unit comprises a nanofiltration device, an evaporation crystallization device and a mother liquor tank which are connected in sequence;
the evaporative crystallization device is also connected with a salt dissolving tank; the mother liquor tank is connected with the carbonization pyrolysis unit; the inlet of the nanofiltration device is connected with the ion exchanger;
the evaporative crystallization device is a four-effect evaporative crystallizer; the four-effect evaporation crystallizer comprises a first effect evaporator 1, a second effect evaporator 2, a third effect evaporator 3 and a fourth effect evaporator 4 which are connected in sequence; refined salt slurry outlets are formed in the bottoms of the second effect evaporator 2 and the fourth effect evaporator 4;
and a water production outlet and a concentrated water outlet of the nanofiltration device 5 are respectively connected with feed inlets of the third-effect evaporator 3 and the first-effect evaporator 1.
Example 3
On the basis of the embodiment 2, the carbonization pyrolysis unit comprises a primary pyrolysis device and a secondary pyrolysis device which are sequentially connected, and the primary pyrolysis device and the secondary pyrolysis device are both connected with the tail gas purification unit; the secondary pyrolysis device is connected with the salt dissolving tank; the primary pyrolysis device is connected with a mother liquor tank.
Preferably, the primary pyrolysis device and the secondary pyrolysis device are both fixed beds or fluidized beds.
Preferably, the fixed bed is a rotary kiln or a rake furnace.
Preferably, the heating modes of the primary pyrolysis device and the secondary pyrolysis device are electric heating, natural gas heating or microwave heating.
Example 4
On the basis of embodiment 3, the carbonization pyrolysis unit further comprises a first crushing device and a second crushing device, wherein the first crushing device is connected with an inlet of the first-stage pyrolysis device, and the first-stage pyrolysis device is connected with the second-stage pyrolysis device through the second crushing device.
Example 5
On the basis of the embodiment 4, the filtering device is formed by connecting a multi-medium filtering device and an ultrafiltration device, or is one of a tubular ultrafiltration device and an immersed ultrafiltration device.
Preferably, the sludge dewatering device is a filter press.
Preferably, the ion exchanger is a chelating resin ion exchanger.
Preferably, an activated carbon adsorption layer is arranged in the COD removing device.
The specific implementation process of the utility model is as follows:
(1) carbonization and pyrolysis:
the waste salt enters a first crushing device, is crushed until the particle size is smaller than 20mm, then enters a first-stage pyrolysis device, controls the oxygen content to be 0-1%, is heated to 200-500 ℃, preferably 350-400 ℃, enters a second crushing device for crushing again after staying for 20-30 min, enters a second-stage pyrolysis device for deep pyrolysis, supplements air to control the oxygen content to be 3-5%, is heated to 500-800 ℃, preferably 550-600 ℃, and stays for 40-60 min;
pyrolysis gas generated by the first-stage pyrolysis device and the second-stage pyrolysis device enters a tail gas purification unit, and is discharged after being treated to reach the standard;
evaporating and gasifying water in the waste salt through primary pyrolysis, and simultaneously carrying out pre-pyrolysis on the waste salt; air is supplemented during secondary pyrolysis, so that the fast pyrolysis of the organic matters can be promoted;
through the carbonization and pyrolysis, the organic matters in the waste salt are pyrolyzed into combustible gas (CO and H)2、VOCs、NOx、SOx) And a small amount of coke, NO in combustible gasx0 to 0.7wt% of SOxThe content is 0-0.2 wt%; the main components of the waste salt after pyrolysis are inorganic salt and a small amount of carbonized slag;
the tail gas purification unit is treated by adopting the prior art until the tail gas is discharged after reaching the standard, for example, the tail gas purification unit comprises a secondary combustion chamber, a waste heat boiler, a quench tower, a dry deacidification system, a bag-type dust remover, a draught fan, a water washing tower, an alkaline washing tower, a flue gas whitening device and a chimney which are sequentially connected; oxygen-enriched combustion is carried out on pyrolysis gas through a secondary combustion chamber, the pyrolysis gas is heated to 1100 ℃ and stays for more than 2 seconds, high-temperature flue gas at the outlet of the secondary combustion chamber enters a waste heat boiler, is subjected to denitrification and flue gas quenching through the waste heat boiler, is subjected to dry deacidification by adding activated carbon and quicklime, is subjected to dust removal through a bag-type dust remover, enters a water washing tower and an alkaline washing tower through a draught fan for wet deacidification, and is subjected to white removal through flue gas and then is discharged through a chimney up to the standard;
(2) refining saline water:
the method comprises the steps of enabling carbon-containing salt residues obtained by a secondary pyrolysis device to enter a salt dissolving tank, supplementing water with the hardness of less than 10mg/L, stirring and dissolving to obtain saline water with the concentration of 15-25 wt%, enabling the saline water to enter a high-efficiency sedimentation tank, and adding a medicament into the saline water, wherein the medicament is PAC (polyaluminium chloride) and Na (sodium sulfate)2CO3And at least one of NaOH, removing hardness, silicon, partial alkalinity, heavy metal and solid impurities in the brine through precipitation solid-liquid separation, adjusting the pH of the effluent of the high-efficiency sedimentation tank to 6.5-8.5 through sulfuric acid, then feeding the effluent into a filtering device, controlling the turbidity of the produced water of the filtering device to be less than 0.2NTU, and ensuring the concentrated brine COD (chemical oxygen demand) entering a salt separation crystallization unit through a COD removal device and an ion exchanger<100mg/L and the hardness is less than 0.1 mg/L;
backwashing water and filter residues of the filtering device and precipitated sludge generated by the high-efficiency sedimentation tank enter the sludge dewatering device for solid-liquid separation, filtrate generated by the sludge dewatering device is discharged from a liquid outlet and returns to the high-efficiency sedimentation tank through a water return pipe, and the generated sludge enters a sludge recovery tank for later use;
(3) salt separation and crystallization unit:
pumping the strong brine produced by the brine refining unit to a nanofiltration device 5, preliminarily separating sodium chloride and sodium sulfate in water, and obtaining nanofiltration product water rich in sodium chloride and nanofiltration concentrated water rich in sodium sulfate;
nanofiltration concentrated water is pumped into a first-effect evaporator 1 in a four-effect evaporation crystallizer, sequentially passes through the first-effect evaporator 1 and a second-effect evaporator 2, water is condensed and recovered after evaporation, slurry containing sodium sulfate is discharged from a refined salt slurry outlet of the second-effect evaporator 2, and the slurry is centrifuged and dried to finally produce sodium sulfate;
nanofiltration produced water is pumped into a third-effect evaporator 3 in a four-effect evaporation crystallizer, sequentially passes through the third-effect evaporator 3 and a fourth-effect evaporator 4, water is condensed and recovered after evaporation, slurry containing sodium chloride is discharged from a refined salt slurry outlet of the fourth-effect evaporator 4, and the slurry is centrifuged and dried to finally produce sodium chloride;
in the evaporative crystallization process, condensed water recovered by the evaporative crystallization device enters a salt dissolving tank;
in the evaporative crystallization process, some components (COD and the like) can be concentrated and enriched continuously, in order to not influence the stable operation of the evaporative crystallization device, a part of 'aging mother liquor' needs to be pumped out periodically, the generated mother liquor is discharged to a mother liquor tank, and then the generated mother liquor returns to a first-stage pyrolysis device for treatment.
The anhydrous sodium sulfate product obtained after the waste salt is treated at least reaches the industrial anhydrous sodium sulfate (GB/T6009-2014)
The index requirements of qualified products are similar, and the sodium chloride at least meets the index requirements of industrial dry salt (secondary grade) in Industrial salt (GB/T5462-2015).
Claims (10)
1. The utility model provides a waste salt resourceful treatment system, includes consecutive carbomorphism pyrolysis unit, salt solution refining unit, divides salt crystallization unit, its characterized in that:
the brine refining unit comprises a salt dissolving tank, a high-efficiency sedimentation tank, a filtering device, a COD removing device and an ion exchanger which are sequentially connected; the efficient sedimentation tank is provided with a medicament feeding port and a stirring device, the efficient sedimentation tank and the filtering device are both connected with a sludge dewatering device, and the sludge dewatering device is also connected with a sludge recovery tank; the sludge dewatering device is also provided with a liquid outlet, and the liquid outlet is connected with the high-efficiency sedimentation tank through a return pipe.
2. The waste salt recycling treatment system according to claim 1, wherein: the salt separation crystallization unit comprises a nanofiltration device, an evaporation crystallization device and a mother liquor tank which are connected in sequence;
the evaporative crystallization device is also connected with a salt dissolving tank; the mother liquor tank is connected with the carbonization pyrolysis unit; the inlet of the nanofiltration device is connected with the ion exchanger;
the evaporative crystallization device is a four-effect evaporative crystallizer; the four-effect evaporation crystallizer comprises a first effect evaporator (1), a second effect evaporator (2), a third effect evaporator (3) and a fourth effect evaporator (4) which are connected in sequence; refined salt slurry outlets are formed in the bottoms of the second-effect evaporator (2) and the fourth-effect evaporator (4);
and a water production outlet and a concentrated water outlet of the nanofiltration device (5) are respectively connected with feed inlets of the third-effect evaporator (3) and the first-effect evaporator (1).
3. The waste salt recycling treatment system according to claim 2, wherein: the carbonization pyrolysis unit comprises a primary pyrolysis device and a secondary pyrolysis device which are sequentially connected, and the primary pyrolysis device and the secondary pyrolysis device are both connected with the tail gas purification unit; the secondary pyrolysis device is connected with the salt dissolving tank; the primary pyrolysis device is connected with a mother liquor tank.
4. The waste salt recycling treatment system according to claim 3, wherein: the first-stage pyrolysis device and the second-stage pyrolysis device are both fixed beds or fluidized beds.
5. The waste salt recycling treatment system according to claim 4, wherein: the fixed bed is a rotary kiln or a rake furnace.
6. The waste salt recycling treatment system according to claim 4, wherein: the heating modes of the first-stage pyrolysis device and the second-stage pyrolysis device are electric heating, natural gas heating or microwave heating.
7. The waste salt recycling treatment system according to claim 3, wherein: the carbonization pyrolysis unit further comprises a first crushing device and a second crushing device, the first crushing device is connected with an inlet of the first-stage pyrolysis device, and the first-stage pyrolysis device and the second-stage pyrolysis device are connected through the second crushing device.
8. The waste salt recycling treatment system according to claim 1, wherein: the filtering device is formed by connecting a multi-medium filtering device and an ultrafiltration device, or is one of a tubular ultrafiltration device and an immersed ultrafiltration device.
9. The waste salt recycling treatment system according to claim 1, wherein: the sludge dewatering device is a filter press.
10. The waste salt recycling treatment system according to claim 1, wherein: the ion exchanger is a chelating resin ion exchanger.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202121925274.3U CN215391554U (en) | 2021-08-17 | 2021-08-17 | Waste salt resourceful treatment system |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202121925274.3U CN215391554U (en) | 2021-08-17 | 2021-08-17 | Waste salt resourceful treatment system |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113510140A (en) * | 2021-08-17 | 2021-10-19 | 陕西省石油化工研究设计院 | Waste salt recycling treatment system and method |
| CN117487594A (en) * | 2023-12-29 | 2024-02-02 | 呼伦贝尔金新化工有限公司 | Novel fluxing agent adding system and method for lignite pressurized gasification |
-
2021
- 2021-08-17 CN CN202121925274.3U patent/CN215391554U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113510140A (en) * | 2021-08-17 | 2021-10-19 | 陕西省石油化工研究设计院 | Waste salt recycling treatment system and method |
| CN113510140B (en) * | 2021-08-17 | 2024-05-14 | 陕西化工研究院有限公司 | Waste salt recycling treatment system and method |
| CN117487594A (en) * | 2023-12-29 | 2024-02-02 | 呼伦贝尔金新化工有限公司 | Novel fluxing agent adding system and method for lignite pressurized gasification |
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