CN112691509A - Equipment and method for separating sodium and potassium salts in high-temperature molten flue gas of waste incineration fly ash - Google Patents
Equipment and method for separating sodium and potassium salts in high-temperature molten flue gas of waste incineration fly ash Download PDFInfo
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- CN112691509A CN112691509A CN202110151102.3A CN202110151102A CN112691509A CN 112691509 A CN112691509 A CN 112691509A CN 202110151102 A CN202110151102 A CN 202110151102A CN 112691509 A CN112691509 A CN 112691509A
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 83
- 239000003546 flue gas Substances 0.000 title claims abstract description 83
- 239000010881 fly ash Substances 0.000 title claims abstract description 39
- 238000004056 waste incineration Methods 0.000 title claims abstract description 35
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 title claims abstract description 25
- 229910052708 sodium Inorganic materials 0.000 title claims abstract description 25
- 239000011734 sodium Substances 0.000 title claims abstract description 25
- 159000000001 potassium salts Chemical class 0.000 title claims abstract description 24
- 238000000034 method Methods 0.000 title claims abstract description 17
- 239000007788 liquid Substances 0.000 claims abstract description 56
- 238000002425 crystallisation Methods 0.000 claims abstract description 54
- 230000008025 crystallization Effects 0.000 claims abstract description 53
- WCUXLLCKKVVCTQ-UHFFFAOYSA-M Potassium chloride Chemical compound [Cl-].[K+] WCUXLLCKKVVCTQ-UHFFFAOYSA-M 0.000 claims abstract description 47
- 238000001704 evaporation Methods 0.000 claims abstract description 46
- 230000008020 evaporation Effects 0.000 claims abstract description 40
- 238000000926 separation method Methods 0.000 claims abstract description 39
- 239000002994 raw material Substances 0.000 claims abstract description 32
- 239000001103 potassium chloride Substances 0.000 claims abstract description 31
- 235000011164 potassium chloride Nutrition 0.000 claims abstract description 31
- 238000005507 spraying Methods 0.000 claims abstract description 27
- 238000011033 desalting Methods 0.000 claims abstract description 26
- 159000000000 sodium salts Chemical class 0.000 claims abstract description 21
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 17
- 238000007599 discharging Methods 0.000 claims abstract description 15
- 239000007789 gas Substances 0.000 claims abstract description 13
- 239000012535 impurity Substances 0.000 claims abstract description 8
- 239000000428 dust Substances 0.000 claims abstract description 7
- 238000010612 desalination reaction Methods 0.000 claims abstract description 5
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims description 26
- 239000002562 thickening agent Substances 0.000 claims description 22
- 239000007787 solid Substances 0.000 claims description 20
- 230000001376 precipitating effect Effects 0.000 claims description 18
- 239000000779 smoke Substances 0.000 claims description 18
- 150000003839 salts Chemical class 0.000 claims description 17
- 239000012452 mother liquor Substances 0.000 claims description 16
- 239000011780 sodium chloride Substances 0.000 claims description 13
- 239000013078 crystal Substances 0.000 claims description 11
- 238000002844 melting Methods 0.000 claims description 9
- 230000008018 melting Effects 0.000 claims description 9
- 238000002386 leaching Methods 0.000 claims description 8
- XAEFZNCEHLXOMS-UHFFFAOYSA-M potassium benzoate Chemical compound [K+].[O-]C(=O)C1=CC=CC=C1 XAEFZNCEHLXOMS-UHFFFAOYSA-M 0.000 claims description 6
- 238000004064 recycling Methods 0.000 claims description 6
- 239000007921 spray Substances 0.000 claims description 6
- 230000008569 process Effects 0.000 claims description 5
- 238000010025 steaming Methods 0.000 claims description 5
- 230000004927 fusion Effects 0.000 claims description 4
- 238000005086 pumping Methods 0.000 claims description 4
- 230000008719 thickening Effects 0.000 claims description 4
- 238000001514 detection method Methods 0.000 claims description 3
- 238000001914 filtration Methods 0.000 claims description 3
- 241001397173 Kali <angiosperm> Species 0.000 claims 1
- 239000002956 ash Substances 0.000 claims 1
- 239000000243 solution Substances 0.000 description 30
- 239000002918 waste heat Substances 0.000 description 7
- 230000006872 improvement Effects 0.000 description 6
- 239000000463 material Substances 0.000 description 4
- 239000013589 supplement Substances 0.000 description 3
- HGUFODBRKLSHSI-UHFFFAOYSA-N 2,3,7,8-tetrachloro-dibenzo-p-dioxin Chemical compound O1C2=CC(Cl)=C(Cl)C=C2OC2=C1C=C(Cl)C(Cl)=C2 HGUFODBRKLSHSI-UHFFFAOYSA-N 0.000 description 2
- 241000209094 Oryza Species 0.000 description 2
- 235000007164 Oryza sativa Nutrition 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000004744 fabric Substances 0.000 description 2
- 239000006260 foam Substances 0.000 description 2
- 229910001385 heavy metal Inorganic materials 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 235000009566 rice Nutrition 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- 241000282414 Homo sapiens Species 0.000 description 1
- 229910002651 NO3 Inorganic materials 0.000 description 1
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 1
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical compound OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 238000005119 centrifugation Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
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- 239000011550 stock solution Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 239000002341 toxic gas Substances 0.000 description 1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1418—Recovery of products
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1431—Pretreatment by other processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1431—Pretreatment by other processes
- B01D53/145—Pretreatment by separation of solid or liquid material
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
-
- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/10—Inorganic absorbents
- B01D2252/103—Water
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
- B01D2258/0291—Flue gases from waste incineration plants
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- Chemical & Material Sciences (AREA)
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- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Materials Engineering (AREA)
- Inorganic Chemistry (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention provides equipment and a method for separating sodium and potassium salts in high-temperature molten flue gas of waste incineration fly ash, wherein the equipment comprises a desalting and dedusting device: used for carrying out desalination, denitration and dust removal on the discharged incineration flue gas; flue gas deacidification device: the device is used for deacidifying the flue gas, a spraying device is arranged on the flue gas deacidification device, the spraying device is used for spraying the flue gas to dissolve sodium salt and sylvite into spraying water to obtain a dissolved solution, and the rest tail gas is discharged; a solid-liquid separation device: the device is communicated with a flue gas deacidification device and is used for carrying out solid-liquid separation on a dissolved solution, enabling a raw material solution dissolving sodium salt and sylvite to flow into an evaporation crystallization device through a pipeline, and collecting and discharging insoluble impurities; an evaporation crystallization device: is communicated with a solid-liquid separation device through a pipeline and is used for carrying out evaporation crystallization on the raw material liquid to separate sodium salt and sylvite. The device and the method are used for sorting the sodium and potassium salts in the flue gas, so that the emission is reduced, the flue gas is recycled, and considerable economic benefits are generated.
Description
Technical Field
The invention relates to the technical field of high-temperature melting of waste incineration fly ash, in particular to equipment and a method for separating sodium and potassium salts in high-temperature melting smoke of waste incineration fly ash.
Background
With the development of society, the quality of life of people is better and better, and along with the generation of a large amount of waste incineration fly ash, the waste incineration fly ash treatment methods commonly used at present have the following two types: one is to adopt the landfill technology of the fly ash of the waste incineration, however, with the gradual reduction of the urban land, people are also looking for the scheme of replacing the landfill technology of the fly ash of the waste incineration; the other mode is to burn the fly ash from the incineration of the household garbage, the fly ash from the incineration of the household garbage generates a large amount of toxic gas during the incineration, and the fly ash from the incineration of the household garbage has various types, and the density, shape, chemical property and melting special effect of combustible materials in the fly ash are different, so that many combustible materials in the common incineration mode can not be fully melted, and a large amount of black smoke and harmful gas are generated while the combustible materials are not fully melted, thereby polluting the atmosphere and being harmful to the health of human beings. Meanwhile, the generated waste incineration fly ash is rich in dioxin, heavy metal and other hazards, and the dioxin in the fly ash can be decomposed and most heavy metal can be solidified through melting treatment.
When the waste incineration fly ash is subjected to melting treatment, smoke is generated and discharged, the smoke often contains a lot of sodium chloride and potassium chloride, and the smoke has considerable economic value if being taken as a product, and is wasted if being directly discharged, but the smoke is difficult to separate the two by dust removal and collection. Therefore, an apparatus or method is needed for sorting and recycling potassium chloride and sodium chloride in the flue gas.
Disclosure of Invention
In view of this, the invention provides a device and a method for separating sodium and potassium salts from high-temperature molten flue gas of waste incineration fly ash, and the device and the method are used for separating sodium and potassium salts from flue gas, thereby reducing emission and recycling and generating considerable economic benefits.
The invention solves the technical problems by the following technical means: the invention provides a device for separating sodium and potassium salts from high-temperature molten flue gas of waste incineration fly ash, which comprises a desalting and dedusting device: the device is communicated with a smoke outlet of a waste incineration fly ash fusion treatment device through a pipeline and is used for desalting, denitrating and dedusting the discharged incineration smoke;
flue gas deacidification device: the device is connected with a desalting and dedusting device through a pipeline and is used for deacidifying the flue gas, a spraying device is arranged on the flue gas deacidification device, the flue gas is sprayed through the spraying device, so that sodium salt and sylvite are dissolved in spraying water to obtain a dissolved solution, and the residual tail gas is discharged outside;
a solid-liquid separation device: the device is communicated with a flue gas deacidification device and is used for carrying out solid-liquid separation on a dissolved solution, enabling a raw material solution dissolving sodium salt and sylvite to flow into an evaporation crystallization device through a pipeline, and collecting and discharging insoluble impurities;
an evaporation crystallization device: is communicated with a solid-liquid separation device through a pipeline and is used for carrying out evaporation crystallization on the raw material liquid to separate sodium salt and sylvite.
Further, still include exhaust-heat boiler, exhaust-heat boiler sets up between desalination dust collector and flue gas deacidification device, exhaust-heat boiler is used for retrieving the flue gas and preheats the steam that produces and supply as the steam of evaporation crystallization device.
And the device further comprises a dissolving and precipitating device, wherein the dissolving and precipitating device is arranged between the solid-liquid separation device and the flue gas deacidification device, and is used for dissolving the solid sodium salt and the solid potassium salt separated in the desalting and denitration device into a dissolving solution.
Further, a PH detection device and a PH adjusting device are arranged in the dissolving and precipitating device.
Further, the evaporative crystallization device comprises a preheater, an evaporator, a separator and a compressor, the preheater is communicated with the solid-liquid separation device through a feed pump and a feed pipe and is used for preheating raw material liquid, the evaporator is communicated with the preheater and is used for evaporating the preheated raw material liquid, the evaporator, the separator and the compressor sequentially form a circulation loop through pipeline communication to enable secondary steam generated by evaporation in the separator to enter the compressor and enter the evaporator for heat exchange after being converted by the compressor, an outlet of the separator is connected with a first thickener, the first thickener is communicated with a first centrifugal machine and a second thickener respectively, and the second thickener is communicated with a second centrifugal machine.
Further, the evaporative crystallization device further comprises a single evaporation device, wherein a leaching tank is arranged on the single evaporation device, and the single evaporation device is communicated with a second centrifugal machine.
Further, the evaporative crystallization device is communicated with the spraying device through a pipeline, and a condensate pump is arranged between the evaporative crystallization device and the spraying device and used for recycling condensate generated by the evaporative crystallization device.
The invention also provides a separation method based on the separation equipment for sodium and potassium salts in the high-temperature molten flue gas of the waste incineration fly ash, which comprises the following steps:
s1, conveying incineration flue gas discharged from a smoke outlet of the waste incineration fly ash melting treatment device into a desalting and dedusting device through a pipeline, desalting, denitrating and dedusting through a filter screen, introducing the filtered flue gas into a flue gas deacidification device, and collecting filtered miscellaneous salts and adding the collected miscellaneous salts into a dissolving and precipitating device;
s2, introducing the filtered flue gas into a flue gas deacidification device for spray deacidification to dissolve sodium salt and potassium salt into water, then discharging tail gas, and pumping the dissolved solution into a dissolving and precipitating device through a liquid pump to dissolve miscellaneous salts to form a dissolved solution;
s3, introducing the dissolved solution into a solid-liquid separation device for solid-liquid separation, and discharging insoluble impurities in the dissolved solution out of the residual raw material solution;
and S4, introducing the raw material liquid into an evaporative crystallization device for evaporative crystallization, and respectively crystallizing and separating sodium chloride and potassium chloride.
Further, step S4 includes that S41 the raw material liquid enters a preheater through a feed pump, enters an evaporator and a separator after being preheated, and then is pumped into the evaporator through a circulating pump for continuous circulation, thereby performing evaporation, concentration and crystallization;
s42, in the crystallization process, evaporating and concentrating to separate out solids, wherein the separated out solids are sodium chloride, concentrating to a potassium chloride saturation point, discharging the solids out of the system, allowing the solids to enter a first thickener for thickening, separating sodium chloride crystals by using a first centrifuge, allowing mother liquor centrifuged by using the first centrifuge to enter a second thickener to separate out potassium chloride crystals, and allowing the mother liquor centrifuged by using a second centrifuge to separate out potassium chloride crystals;
and S43, periodically feeding the mother liquor subjected to twice centrifugal separation into a single-steaming device to treat the high-boiling-point mother liquor, and filtering out crystallized miscellaneous salts through a leaching tank.
According to the technical scheme, the invention has the beneficial effects that: the invention provides equipment and a method for separating sodium and potassium salts in high-temperature molten flue gas of waste incineration fly ash, wherein the equipment comprises a desalting and dedusting device: the device is communicated with a smoke outlet of a waste incineration fly ash fusion treatment device through a pipeline and is used for desalting, denitrating and dedusting the discharged incineration smoke; flue gas deacidification device: the device is connected with a desalting and dedusting device through a pipeline and is used for deacidifying the flue gas, a spraying device is arranged on the flue gas deacidification device, the flue gas is sprayed through the spraying device, so that sodium salt and sylvite are dissolved in spraying water to obtain a dissolved solution, and the residual tail gas is discharged outside; a solid-liquid separation device: the device is communicated with a flue gas deacidification device and is used for carrying out solid-liquid separation on a dissolved solution, enabling a raw material solution dissolving sodium salt and sylvite to flow into an evaporation crystallization device through a pipeline, and collecting and discharging insoluble impurities; an evaporation crystallization device: is communicated with a solid-liquid separation device through a pipeline and is used for carrying out evaporation crystallization on the raw material liquid to separate sodium salt and sylvite. The device and the method are used for sorting the sodium and potassium salts in the flue gas, so that the emission is reduced, the flue gas is recycled, and considerable economic benefits are generated.
Drawings
In order to more clearly illustrate the detailed description of the invention or the technical solutions in the prior art, the drawings that are needed in the detailed description of the invention or the prior art will be briefly described below. Throughout the drawings, like elements or portions are generally identified by like reference numerals. In the drawings, elements or portions are not necessarily drawn to scale.
FIG. 1 is a schematic view of a device for separating sodium and potassium salts from high-temperature molten flue gas of waste incineration fly ash provided by the invention;
FIG. 2 is a schematic view of an evaporative crystallization apparatus of a separation device for sodium and potassium salts in high-temperature molten flue gas of waste incineration fly ash according to the present invention;
FIG. 3 is a flow chart of an evaporative crystallization method of the apparatus for separating sodium and potassium salts from high-temperature molten flue gas of waste incineration fly ash according to the present invention;
reference numerals:
1-a desalting and dedusting device; 2-a waste heat boiler; 3-a flue gas deacidification device; 4-dissolving and precipitating device; 5-a solid-liquid separation device; 6-an evaporative crystallization device; 61-a preheater; 62-an evaporator; 63-a compressor; 64-a separator; 65-first thickener; 66-a first centrifuge; 67-second thickener; 68-a second centrifuge; 69-single steaming device; 691-leaching tank.
Detailed Description
Embodiments of the present invention will be described in detail below with reference to the accompanying drawings. The following examples are only for illustrating the technical solutions of the present invention more clearly, and therefore are only examples, and the protection scope of the present invention is not limited thereby.
Referring to fig. 1 to 3, the present invention provides a device for separating sodium and potassium salts from high temperature molten flue gas of waste incineration fly ash, including a desalination and dust removal device 1: the device is communicated with a smoke outlet of a waste incineration fly ash fusion treatment device through a pipeline and is used for desalting, denitrating and dedusting the discharged incineration smoke; the flue gas is discharged from the smoke outlet and then is conveyed into the desalting and dedusting device 1 through a pipeline for desalting and dedusting; the desalting and dedusting device 1 is internally provided with a deduster and an SCR reactor for denitration reaction in sequence, and is used for dedusting and denitration respectively and collecting miscellaneous salt.
Flue gas deacidification device 3: the flue gas deacidification device 3 is provided with a spraying device, and the spraying device is used for spraying the flue gas to dissolve sodium salt and sylvite into spraying water to obtain a dissolved solution, and discharging the residual tail gas; the flue gas deacidification device 3 comprises a tower drum, wherein an upper end enclosure with an exhaust pipe is arranged at the top of the tower drum, a lower end enclosure with an air inlet pipe is arranged at the bottom of the tower drum, a spraying liquid taking port is arranged on the side wall of the tower drum, and a spraying pipeline system with a spraying pump is arranged outside the tower drum; the inside riser that communicates in the intake pipe that is equipped with, riser upper end be equipped with inside intercommunication and have the gas distribution awl of gas distribution hole, the top of gas distribution awl is equipped with the baffling cap, the top of baffling cap is equipped with the foam and takes place the cover, the top that the cover was taken place to the foam is equipped with the cloth liquid system, cloth liquid system top is equipped with defoaming system, defoaming system's top is equipped with the defroster, low head below be equipped with the drain.
Solid-liquid separation device 5: the device is communicated with the flue gas deacidification device 3 and is used for carrying out solid-liquid separation on the dissolved solution, leading the raw material solution dissolving sodium salt and sylvite to flow into an evaporation crystallization device 6 through a pipeline, and collecting and discharging insoluble impurities;
the evaporative crystallization device 6: is communicated with a solid-liquid separation device 5 through a pipeline and is used for carrying out evaporation crystallization on the raw material liquid to separate sodium salt and sylvite. The evaporative crystallization device 6 adopts an MVR evaporation mode, secondary steam generated by compression and evaporation of the high-energy-efficiency steam compressor 63 is used for converting a computer into heat energy, the enthalpy of the secondary steam is improved, and the secondary steam with the improved heat energy is pumped into the evaporator 62 for heating so as to achieve the purpose of realizing evaporative crystallization by recycling the existing heat energy of the secondary steam through self-circulation of the evaporator 62. More contain energy and condensate water, reduce area simultaneously.
As a further improvement to the above technical scheme, the system further comprises a waste heat boiler 2, wherein the waste heat boiler 2 is arranged between the desalting and dedusting device 1 and the flue gas deacidification device 3, and the waste heat boiler 2 is used for recovering flue gas and preheating the generated steam to supplement the steam of the evaporation and crystallization device 6. The incineration flue gas temperature after desalination and dust removal exceeds 350 ℃, a large amount of heat waste can be caused by directly entering the flue gas deacidification device 3, and the manufacturing cost of rear-end equipment can be greatly improved. A preheating recovery boiler is arranged in front of the deacidification device, steam generated by recovery and preheating is used as steam supplement of the rear-end evaporation crystallization device 6, energy is effectively utilized, and direct economic benefits are generated. The gas outlet of the waste heat boiler 2 is communicated with the flue gas deacidification device 3, and the steam outlet of the waste heat boiler 2 is communicated with the evaporative crystallization device 6 for steam supplement. The steam outlet of the waste heat boiler 2 can also be connected with a generator to generate electricity.
As a further improvement of the above technical solution, the device further comprises a dissolving and precipitating device 4, wherein the dissolving and precipitating device 4 is arranged between the solid-liquid separation device 5 and the flue gas deacidification device 3, and the dissolving and precipitating device 4 is used for dissolving the solid sodium salt and the solid potassium salt separated in the desalting and denitration device into the dissolving solution. And a dissolving and precipitating device 4 is arranged, and the spray water after deacidification of the flue gas is used for dissolving the miscellaneous salt obtained in the desalting and dedusting process, so that the sodium and potassium salts in the miscellaneous salt can be conveniently and synchronously separated and crystallized. The water consumption is reduced, and the energy is saved.
As a further improvement to the technical scheme, a PH detection device and a PH adjusting device are arranged in the dissolving and precipitating device 4.
As a further improvement of the above technical solution, the evaporative crystallization device 6 includes a preheater 61, an evaporator 62, a separator 64, and a compressor 63, the preheater 61 is communicated with the solid-liquid separation device 5 through a feed pump and a feed pipe, and is used for preheating the raw material liquid, the evaporator 62 is communicated with the preheater 61, and is used for evaporating the preheated raw material liquid, the evaporator 62, the separator 64, and the compressor 63 are sequentially communicated through a pipeline to form a circulation loop, so that the secondary steam generated by evaporation in the separator 64 enters the compressor 63, is converted by the compressor 63, and then enters the evaporator 62 for heat exchange, an outlet of the separator 64 is connected with a first thickener 65, the first thickener 65 is respectively communicated with a first centrifuge 66 and a second thickener 67, and the second thickener 67 is communicated with a second centrifuge 68. The raw material liquid after solid-liquid separation enters a preheater 61 through a feed pump to be preheated and then is transferred into an evaporator 62 and a separator 64, then the raw material liquid is pumped into the evaporator 62 through a circulating pump to continuously circulate to achieve the purpose of rice steaming concentration and crystallization, meanwhile, secondary steam generated by rice steaming in the separator 64 enters a compressor 63, and is converted into high-grade steam after being compressed by the compressor 63 to enter the evaporator 62 for heat exchange. Meanwhile, compressed steam enters the evaporator 62 to release heat and then condensed water in a condensation layer is discharged to the preheater 61 through a condensed water pump to exchange heat with feed, and the condensed water after heat exchange is discharged into a spraying device to be recycled as spraying water, so that energy is saved. The connecting pipeline between the adjacent devices is respectively provided with a circulating pump or a raw material pump for driving the circulation of the flue gas or the raw material liquid, wherein the circulating pump is used for driving the circulation of the raw material, for example, the circulating pump is arranged between the heater and the separator so as to make the raw material circularly flow.
The potassium chloride solubility is obviously recorded along with the temperature change and is higher, during evaporation concentration, the evaporation concentration is firstly carried out until solid is separated out, at the moment, the separated-out solid is sodium chloride, the concentration is continuously carried out until the concentration is close to the saturation point of the potassium chloride, the mixture is discharged out of the system and enters a first thickener 65 for thickening, and sodium chloride crystals are separated out through a first centrifuge 66 to obtain sodium chloride; the centrifuged mother liquor enters a second thickener 67, and is cooled by using circulating water, potassium chloride crystals are separated out from the solution and enter a second centrifuge 68 to be separated out, and the mother liquor after twice centrifugation is preheated after returning to the front end and mixing with the stock solution and then returns to the evaporative crystallization device 6 to be continuously evaporated.
As a further improvement to the above technical solution, the evaporative crystallization apparatus 6 further includes a single evaporation apparatus 69, the single evaporation apparatus 69 is provided with a leaching tank 691, and the single evaporation apparatus 69 is communicated with the second centrifuge 68. In the operation process of the evaporation system, high-boiling-point substances such as nitrate, sulfite and the like brought by spraying wastewater can be continuously concentrated and exceed the temperature rise of the compressor 63, a set of single evaporation device 69 is arranged for treating high-boiling-point mother liquor, part of high-temperature mother liquor is periodically discharged and treated in the single evaporation device 69, and miscellaneous salts are removed through the leaching tank 691, so that zero discharge of wastewater is realized.
As a further improvement of the above technical solution, the evaporative crystallization device 6 is further communicated with a spray device through a pipeline, and a condensate pump is arranged between the evaporative crystallization device 6 and the spray device for recycling condensate generated by the evaporative crystallization device 6.
The invention also provides a separation method based on the separation equipment for sodium and potassium salts in the high-temperature molten flue gas of the waste incineration fly ash, which comprises the following steps:
s1, conveying incineration flue gas discharged from a smoke outlet of the waste incineration fly ash melting treatment device into a desalting and dedusting device 1 through a pipeline, desalting, denitrating and dedusting through a filter screen, introducing the filtered flue gas into a flue gas deacidification device 3, and collecting filtered miscellaneous salts and adding the collected miscellaneous salts into a dissolving and precipitating device 4;
s2, introducing the filtered flue gas into a flue gas deacidification device 3 for spray deacidification to dissolve sodium salt and potassium salt into water, then discharging tail gas, and pumping the dissolved solution into a dissolving and precipitating device 4 through a liquid pump to dissolve miscellaneous salts to form a dissolved solution;
s3, introducing the dissolved solution into a solid-liquid separation device 5 for solid-liquid separation, and discharging insoluble impurities in the dissolved solution out of the residual raw material solution;
s4, introducing the raw material liquid into an evaporative crystallization device 6 for evaporative crystallization; s41, feeding the raw material liquid into a preheater 61 through a feeding pump, preheating, feeding the raw material liquid into an evaporator 62 and a separator 64, and pumping the material into the evaporator 62 through a circulating pump for continuous circulation so as to carry out evaporation, concentration and crystallization;
s42, in the crystallization process, evaporating and concentrating to separate out solids, wherein the separated out solids are sodium chloride, concentrating to a potassium chloride saturation point, discharging the solids out of the system, allowing the solids to enter a first thickener 65 for thickening, separating sodium chloride crystals by using a first centrifuge 66, allowing the mother liquor centrifuged by the first centrifuge 66 to enter a second thickener 67 for separating out potassium chloride crystals, and allowing the mother liquor to enter a second centrifuge 68 for separating out potassium chloride crystals;
s43, periodically feeding the mother liquor after twice centrifugal separation into a single evaporator 69 to treat the high boiling point mother liquor, and filtering out crystallized miscellaneous salts through a leaching tank 691.
Finally, it should be noted that: the above embodiments are only used to illustrate the technical solution of the present invention, and not to limit the same; while the invention has been described in detail and with reference to the foregoing embodiments, it will be understood by those skilled in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; such modifications and substitutions do not depart from the spirit and scope of the present invention, and they should be construed as being included in the following claims and description.
Claims (9)
1. The utility model provides a sodium kali salt splitter in waste incineration flying ash high temperature melting flue gas which characterized in that: comprises that
A desalting and dust removing device: the device is communicated with a smoke outlet of a waste incineration fly ash fusion treatment device through a pipeline and is used for desalting, denitrating and dedusting the discharged incineration smoke;
flue gas deacidification device: the device is connected with a desalting and dedusting device through a pipeline and is used for deacidifying the flue gas, a spraying device is arranged on the flue gas deacidification device, the flue gas is sprayed through the spraying device, so that sodium salt and sylvite are dissolved in spraying water to obtain a dissolved solution, and the residual tail gas is discharged outside;
a solid-liquid separation device: the device is communicated with a flue gas deacidification device and is used for carrying out solid-liquid separation on a dissolved solution, enabling a raw material solution dissolving sodium salt and sylvite to flow into an evaporation crystallization device through a pipeline, and collecting and discharging insoluble impurities;
an evaporation crystallization device: is communicated with a solid-liquid separation device through a pipeline and is used for carrying out evaporation crystallization on the raw material liquid to separate sodium salt and sylvite.
2. The apparatus for separating sodium and potassium salts from high-temperature molten flue gas of waste incineration fly ash according to claim 1, characterized in that: still include exhaust-heat boiler, exhaust-heat boiler sets up between desalination dust collector and flue gas deacidification device, exhaust-heat boiler is used for retrieving the flue gas and preheats the steam that produces and supply as the steam of evaporation crystallization device.
3. The apparatus for separating sodium and potassium salts from high-temperature molten flue gas of waste incineration fly ash according to claim 1, characterized in that: the device also comprises a dissolving and precipitating device, wherein the dissolving and precipitating device is arranged between the solid-liquid separation device and the flue gas deacidification device, and is used for dissolving the solid sodium salt and the solid potassium salt separated in the desalting and denitration device into a dissolving solution.
4. The apparatus for separating sodium and potassium salts from high-temperature molten flue gas of waste incineration fly ash according to claim 3, characterized in that: and a PH detection device and a PH adjusting device are arranged in the dissolving and precipitating device.
5. The apparatus for separating sodium and potassium salts from high-temperature molten flue gas of waste incineration fly ash according to claim 1, characterized in that: the evaporative crystallization device comprises a preheater, an evaporator, a separator and a compressor, wherein the preheater is communicated with a solid-liquid separation device through a feed pump and a feed pipe and is used for preheating raw material liquid, the evaporator is communicated with the preheater and is used for evaporating the preheated raw material liquid, the evaporator, the separator and the compressor are sequentially communicated through a pipeline to form a circulation loop so that secondary steam generated by evaporation in the separator enters the compressor to be converted by the compressor and then enters the evaporator to exchange heat, an outlet of the separator is connected with a first thickener, the first thickener is communicated with a first centrifugal machine and a second thickener respectively, and the second thickener is communicated with a second centrifugal machine.
6. The apparatus for separating sodium and potassium salts from high-temperature molten flue gas of waste incineration fly ash according to claim 5, characterized in that: the evaporative crystallization device further comprises a single evaporation device, wherein a leaching tank is arranged on the single evaporation device, and the single evaporation device is communicated with the second centrifugal machine.
7. The apparatus for separating sodium and potassium salts from high-temperature molten flue gas of waste incineration fly ash according to claim 1, characterized in that: the evaporative crystallization device is also communicated with the spraying device through a pipeline, and a condensate pump is arranged between the evaporative crystallization device and the spraying device and used for recycling condensate water generated by the evaporative crystallization device.
8. The separation method of the equipment for separating the sodium and potassium salts in the high-temperature molten flue gas of the waste incineration fly ash based on the claims 1-7 is characterized by comprising the following steps: the method comprises the following steps:
s1, conveying incineration flue gas discharged from a smoke outlet of the waste incineration fly ash melting treatment device into a desalting and dedusting device through a pipeline, desalting, denitrating and dedusting through a filter screen, introducing the filtered flue gas into a flue gas deacidification device, and collecting filtered miscellaneous salts and adding the collected miscellaneous salts into a dissolving and precipitating device;
s2, introducing the filtered flue gas into a flue gas deacidification device for spray deacidification to dissolve sodium salt and potassium salt into water, then discharging tail gas, and pumping the dissolved solution into a dissolving and precipitating device through a liquid pump to dissolve miscellaneous salts to form a dissolved solution;
s3, introducing the dissolved solution into a solid-liquid separation device for solid-liquid separation, and discharging insoluble impurities in the dissolved solution out of the residual raw material solution;
and S4, introducing the raw material liquid into an evaporative crystallization device for evaporative crystallization, and respectively crystallizing and separating sodium chloride and potassium chloride.
9. The separation method according to claim 8, characterized in that: step S4 also comprises the steps that S41, the raw material liquid enters a preheater through a feed pump, enters an evaporator and a separator after being preheated, and then is pumped into the evaporator for continuous circulation through a circulating pump, so that evaporation, concentration and crystallization are carried out;
s42, in the crystallization process, evaporating and concentrating to separate out solids, wherein the separated out solids are sodium chloride, concentrating to a potassium chloride saturation point, discharging the solids out of the system, allowing the solids to enter a first thickener for thickening, separating sodium chloride crystals by using a first centrifuge, allowing mother liquor centrifuged by using the first centrifuge to enter a second thickener to separate out potassium chloride crystals, and allowing the mother liquor centrifuged by using a second centrifuge to separate out potassium chloride crystals;
and S43, periodically feeding the mother liquor subjected to twice centrifugal separation into a single-steaming device to treat the high-boiling-point mother liquor, and filtering out crystallized miscellaneous salts through a leaching tank.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113546944A (en) * | 2021-07-14 | 2021-10-26 | 北京科技大学 | Method for degrading dioxin in waste incineration fly ash and recycling potassium and sodium elements |
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