CN111672879A - Waste salt recycling system and method based on energy conservation and environment protection integration of thermal power plant - Google Patents
Waste salt recycling system and method based on energy conservation and environment protection integration of thermal power plant Download PDFInfo
- Publication number
- CN111672879A CN111672879A CN202010562203.5A CN202010562203A CN111672879A CN 111672879 A CN111672879 A CN 111672879A CN 202010562203 A CN202010562203 A CN 202010562203A CN 111672879 A CN111672879 A CN 111672879A
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- outlet
- inlet
- salt
- temperature
- heat exchanger
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- 150000003839 salts Chemical class 0.000 title claims abstract description 131
- 239000002699 waste material Substances 0.000 title claims abstract description 99
- 238000000034 method Methods 0.000 title claims abstract description 41
- 238000004064 recycling Methods 0.000 title claims abstract description 17
- 230000010354 integration Effects 0.000 title claims abstract description 12
- 238000004134 energy conservation Methods 0.000 title claims abstract description 9
- 239000007788 liquid Substances 0.000 claims abstract description 81
- 239000000428 dust Substances 0.000 claims abstract description 66
- 238000001179 sorption measurement Methods 0.000 claims abstract description 53
- 239000013078 crystal Substances 0.000 claims abstract description 46
- 238000007710 freezing Methods 0.000 claims abstract description 44
- 230000008014 freezing Effects 0.000 claims abstract description 44
- 230000001112 coagulating effect Effects 0.000 claims abstract description 37
- 238000002425 crystallisation Methods 0.000 claims abstract description 36
- 230000008025 crystallization Effects 0.000 claims abstract description 36
- 238000001556 precipitation Methods 0.000 claims abstract description 36
- 238000004062 sedimentation Methods 0.000 claims abstract description 34
- 230000001105 regulatory effect Effects 0.000 claims abstract description 33
- 239000007800 oxidant agent Substances 0.000 claims abstract description 21
- 230000008569 process Effects 0.000 claims abstract description 12
- 230000007613 environmental effect Effects 0.000 claims abstract description 7
- 235000002639 sodium chloride Nutrition 0.000 claims description 143
- 239000007789 gas Substances 0.000 claims description 74
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 71
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 48
- 238000001704 evaporation Methods 0.000 claims description 46
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims description 39
- 230000008020 evaporation Effects 0.000 claims description 38
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 claims description 33
- 239000012266 salt solution Substances 0.000 claims description 32
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 claims description 30
- 239000000243 solution Substances 0.000 claims description 30
- 229910052938 sodium sulfate Inorganic materials 0.000 claims description 28
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 claims description 27
- 235000011152 sodium sulphate Nutrition 0.000 claims description 26
- 238000004458 analytical method Methods 0.000 claims description 24
- 239000002253 acid Substances 0.000 claims description 23
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 22
- 239000002131 composite material Substances 0.000 claims description 22
- 239000007787 solid Substances 0.000 claims description 22
- WCUXLLCKKVVCTQ-UHFFFAOYSA-M Potassium chloride Chemical compound [Cl-].[K+] WCUXLLCKKVVCTQ-UHFFFAOYSA-M 0.000 claims description 20
- 239000012452 mother liquor Substances 0.000 claims description 20
- 238000000197 pyrolysis Methods 0.000 claims description 19
- 239000011780 sodium chloride Substances 0.000 claims description 17
- CDBYLPFSWZWCQE-UHFFFAOYSA-L sodium carbonate Substances [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 16
- 229910000019 calcium carbonate Inorganic materials 0.000 claims description 15
- 239000003054 catalyst Substances 0.000 claims description 15
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 14
- 238000001035 drying Methods 0.000 claims description 13
- 238000006243 chemical reaction Methods 0.000 claims description 11
- 239000003795 chemical substances by application Substances 0.000 claims description 11
- 238000003795 desorption Methods 0.000 claims description 10
- 239000001103 potassium chloride Substances 0.000 claims description 10
- 235000011164 potassium chloride Nutrition 0.000 claims description 10
- 238000005057 refrigeration Methods 0.000 claims description 10
- GFNGCDBZVSLSFT-UHFFFAOYSA-N titanium vanadium Chemical compound [Ti].[V] GFNGCDBZVSLSFT-UHFFFAOYSA-N 0.000 claims description 10
- 238000006477 desulfuration reaction Methods 0.000 claims description 9
- 230000023556 desulfurization Effects 0.000 claims description 9
- 230000003647 oxidation Effects 0.000 claims description 9
- 238000007254 oxidation reaction Methods 0.000 claims description 9
- 239000000126 substance Substances 0.000 claims description 9
- 238000004090 dissolution Methods 0.000 claims description 8
- 239000003814 drug Substances 0.000 claims description 8
- 238000004519 manufacturing process Methods 0.000 claims description 8
- 239000002245 particle Substances 0.000 claims description 8
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 8
- 239000002910 solid waste Substances 0.000 claims description 8
- 239000003463 adsorbent Substances 0.000 claims description 7
- 229910052757 nitrogen Inorganic materials 0.000 claims description 7
- 238000003825 pressing Methods 0.000 claims description 7
- 239000002002 slurry Substances 0.000 claims description 7
- 230000009471 action Effects 0.000 claims description 6
- 229910001385 heavy metal Inorganic materials 0.000 claims description 6
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 claims description 6
- 229910000041 hydrogen chloride Inorganic materials 0.000 claims description 6
- 238000000926 separation method Methods 0.000 claims description 6
- IVORCBKUUYGUOL-UHFFFAOYSA-N 1-ethynyl-2,4-dimethoxybenzene Chemical compound COC1=CC=C(C#C)C(OC)=C1 IVORCBKUUYGUOL-UHFFFAOYSA-N 0.000 claims description 5
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 5
- KRHYYFGTRYWZRS-UHFFFAOYSA-N Fluorane Chemical compound F KRHYYFGTRYWZRS-UHFFFAOYSA-N 0.000 claims description 5
- 238000007599 discharging Methods 0.000 claims description 5
- 239000003546 flue gas Substances 0.000 claims description 5
- 229910000040 hydrogen fluoride Inorganic materials 0.000 claims description 5
- 239000002893 slag Substances 0.000 claims description 5
- 239000002912 waste gas Substances 0.000 claims description 5
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 claims description 4
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 4
- 229910001424 calcium ion Inorganic materials 0.000 claims description 4
- 159000000007 calcium salts Chemical class 0.000 claims description 4
- 150000001768 cations Chemical class 0.000 claims description 4
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- 239000000203 mixture Substances 0.000 claims description 4
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- PUZPDOWCWNUUKD-UHFFFAOYSA-M sodium fluoride Chemical compound [F-].[Na+] PUZPDOWCWNUUKD-UHFFFAOYSA-M 0.000 claims description 4
- VWDWKYIASSYTQR-UHFFFAOYSA-N sodium nitrate Chemical compound [Na+].[O-][N+]([O-])=O VWDWKYIASSYTQR-UHFFFAOYSA-N 0.000 claims description 4
- RSIJVJUOQBWMIM-UHFFFAOYSA-L sodium sulfate decahydrate Chemical compound O.O.O.O.O.O.O.O.O.O.[Na+].[Na+].[O-]S([O-])(=O)=O RSIJVJUOQBWMIM-UHFFFAOYSA-L 0.000 claims description 4
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 claims description 3
- 238000009835 boiling Methods 0.000 claims description 3
- 229910001425 magnesium ion Inorganic materials 0.000 claims description 3
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 claims description 2
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 2
- 239000000920 calcium hydroxide Substances 0.000 claims description 2
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims description 2
- 239000001569 carbon dioxide Substances 0.000 claims description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 2
- 239000000701 coagulant Substances 0.000 claims description 2
- 150000001875 compounds Chemical class 0.000 claims description 2
- 239000008394 flocculating agent Substances 0.000 claims description 2
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 claims description 2
- 239000011775 sodium fluoride Substances 0.000 claims description 2
- 235000013024 sodium fluoride Nutrition 0.000 claims description 2
- 239000004317 sodium nitrate Substances 0.000 claims description 2
- 235000010344 sodium nitrate Nutrition 0.000 claims description 2
- 238000001291 vacuum drying Methods 0.000 claims description 2
- 238000005189 flocculation Methods 0.000 claims 1
- 230000016615 flocculation Effects 0.000 claims 1
- 239000002920 hazardous waste Substances 0.000 abstract description 8
- 238000011084 recovery Methods 0.000 abstract description 7
- 238000005265 energy consumption Methods 0.000 abstract description 4
- 239000002918 waste heat Substances 0.000 abstract description 4
- 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 abstract 1
- 239000000779 smoke Substances 0.000 abstract 1
- 238000001816 cooling Methods 0.000 description 19
- 238000005485 electric heating Methods 0.000 description 12
- 238000005516 engineering process Methods 0.000 description 10
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- 238000005260 corrosion Methods 0.000 description 8
- KVGZZAHHUNAVKZ-UHFFFAOYSA-N 1,4-Dioxin Chemical compound O1C=COC=C1 KVGZZAHHUNAVKZ-UHFFFAOYSA-N 0.000 description 7
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 6
- 229910052799 carbon Inorganic materials 0.000 description 6
- 230000003750 conditioning effect Effects 0.000 description 6
- 239000002440 industrial waste Substances 0.000 description 6
- 238000010438 heat treatment Methods 0.000 description 5
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 4
- -1 hydroxide radicals Chemical class 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
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- 239000000956 alloy Substances 0.000 description 2
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- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
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- 206010021143 Hypoxia Diseases 0.000 description 1
- 235000019738 Limestone Nutrition 0.000 description 1
- UIIMBOGNXHQVGW-DEQYMQKBSA-M Sodium bicarbonate-14C Chemical compound [Na+].O[14C]([O-])=O UIIMBOGNXHQVGW-DEQYMQKBSA-M 0.000 description 1
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Images
Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
- B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D46/00—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours
- B01D46/0027—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours with additional separating or treating functions
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D46/00—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours
- B01D46/24—Particle separators, e.g. dust precipitators, using rigid hollow filter bodies
-
- 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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/38—Removing components of undefined structure
- B01D53/40—Acidic components
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/52—Hydrogen sulfide
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
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- B01D53/34—Chemical or biological purification of waste gases
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- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8603—Removing sulfur compounds
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- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
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- B01D53/8603—Removing sulfur compounds
- B01D53/8606—Removing sulfur compounds only one sulfur compound other than sulfur oxides or hydrogen sulfide
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
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- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8621—Removing nitrogen compounds
- B01D53/8625—Nitrogen oxides
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
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- B01D53/8662—Organic halogen compounds
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D3/00—Halides of sodium, potassium or alkali metals in general
- C01D3/04—Chlorides
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D3/00—Halides of sodium, potassium or alkali metals in general
- C01D3/22—Preparation in the form of granules, pieces, or other shaped products
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- 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
- C01D5/004—Preparation in the form of granules, pieces or other shaped products
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
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Abstract
The invention relates to a waste salt recycling system and method based on energy conservation and environmental protection integration of a thermal power plant, wherein the system comprises: the device comprises a dryer A, a dust and deacidification device B, a vacuum device C, a liquid-liquid heat exchanger D, a solid-liquid heat exchanger E, a high-temperature pyrolyzer F, a negative pressure fan G, a dust and deacidification device H, a dissolving tank K, a coagulating sedimentation tank J, a filter press I, a seed crystal precipitation device O, a regulating tank S, an oxidizer T, a regulating tank U, a freezing crystallization device R, a redissolving tank N, an evaporative crystallizer M, a steam ejector X, an evaporative crystallizer Q, an analytical device L, an adsorption device P, a freezing device V, an evaporative crystallizer W and a draught fan Z. The method can realize harmless and resource treatment of the hazardous waste salt produced industrially based on the thermal process of energy cascade utilization and waste heat recovery, eliminate secondary pollution such as associated dioxin, hazardous waste smoke dust and the like, and remarkably reduce the effective operation energy consumption of the resource treatment of the hazardous waste salt and the treatment cost of the hazardous waste salt.
Description
Technical Field
The invention relates to a waste salt recycling system and method based on energy conservation and environmental protection integration of a thermal power plant, in particular to a method for cooperatively treating high-salt dangerous waste by utilizing waste heat resources of the thermal power plant.
Background
The industrial waste salt is from the industries of pesticide, dye, pharmaceutical chemicals, coal chemicals, steel, metallurgy, refining, coking and the like, is a byproduct in industrial process and is a crystallization product from zero discharge of sewage, and the annual byproduct of industrial waste salt in China exceeds thousands of tons, most of the hazardous waste salt is not properly treated, so that the industrial waste salt is extremely harmful to the environment, and along with the increasingly strengthened treatment of high-salinity wastewater in China, the production amount of the industrial waste salt is increased, and the harmless and recycling treatment of the industrial waste salt is increasingly urgent.
The main technical route of resource treatment of industrial waste salt in China is mainly a technical route of carbonizing and oxidizing organic matters in the waste salt in a mode of burning the waste salt by a thermal method or even melting the waste salt at high temperature, removing the organic matters in the waste salt, purifying multivalent cations by a chemical method, performing a salt separation process by a membrane method and performing crystallization and purification by combining an evaporation method, wherein the fuel burned by the thermal method is mainly natural gas at present, and the existing whole technical route has the problems of high operation cost, large investment, incomplete resource utilization and secondary environmental pollution, particularly has no industrial unified standard and detection means for tail gas treatment of waste salt burned by industry, has no effective technical means for monitoring and treatment, component analysis and the like of dioxin in the tail gas, does not determine the generation mechanism, the generation amount, the components and the like of the dioxin, and is simply applied to the conventional flue gas purification treatment process, The treatment effect is difficult to ensure, and further, the atmospheric pollution is caused; the problems that crystallized salt is scarred, blocked and corroded in a process pipeline, the equipment replacement rate is high, and part of superfine crystallized salt particles escape to the atmosphere in the form of aerosol exist in the operation of equipment, the generation factor of haze is increased invisibly, meanwhile, the treatment cost is high due to overhigh energy consumption, about 8% of dangerous waste residues still exist after the resource treatment of the waste salt and need to be cured and buried, and the expensive landfill treatment cost is high, so that enterprises producing the waste salt can bear no burden; the soluble property of the waste salt causes the waste salt to be unsuitable for landfill, and the waste salt has extremely high landfill requirement and high cost.
Disclosure of Invention
Aiming at the technical problems, the invention provides a waste salt recycling system and method based on energy conservation and environmental protection integration of a thermal power plant.
The specific description of the invention is: the utility model provides a waste salt resource system based on energy-concerving and environment-protective integration of thermal power plant which characterized in that includes: the device comprises a dryer A, a dust and deacidification device B, a vacuum device C, a liquid-liquid heat exchanger D, a solid-liquid heat exchanger E, a high-temperature pyrolyzer F, a negative pressure fan G, a dust and deacidification device H, a dissolving tank K, a coagulating sedimentation tank J, a filter press I, a seed crystal precipitation device O, a regulating tank S, an oxidizer T, a regulating tank U, a freezing crystallization device R, a redissolving tank N, an evaporative crystallizer M, a steam ejector X, an evaporative crystallizer Q, an analytical device L, an adsorption device P, a freezing device V, an evaporative crystallizer W and a draught fan Z. Wherein the content of the first and second substances,
a first inlet 1 of the dryer A is a waste salt inlet, a first outlet 2 of the dryer A is a dried waste salt outlet and is connected with a first inlet 18 of the high-temperature pyrolyzer F, and a second outlet 3 of the dryer A is a dried tail gas outlet and is connected with an inlet 4 of the dedusting deacidifier B;
a first outlet 6 of the dust and deacidification device B is a waste gas outlet after dust removal and deacidification and is connected with an inlet 7 of a vacuum device C, a second outlet 5 of the dust and deacidification device B and a first outlet 24 of the dust and deacidification device H are solid waste outlets and are connected with a second inlet 19 of the high-temperature pyrolyzer F, and a second outlet 25 of the dust and deacidification device H is a waste gas outlet after dust removal and deacidification and is connected with a first inlet 91 of a draught fan Z through a pipeline; the non-condensable gas outlet 8 of the vacuum device C is connected with a second inlet 90 of the induced draft fan Z through a pipeline, an outlet 92 of the induced draft fan Z is a gas outlet, and gas is introduced into a power plant boiler.
A first outlet 20 of the high-temperature pyrolyzer F is a pyrolysis gas outlet and is connected with an inlet 23 of the dedusting deacidification device H through an inlet 21 of a negative pressure fan G, and a second outlet 17 of the high-temperature pyrolyzer F is a hot waste salt outlet and is connected with a first inlet 16 of the solid-liquid heat exchanger E;
a first outlet 15 of the solid-liquid heat exchanger E is an outlet of cooled waste salt and is connected with an inlet 26 of the dissolving tank K, a second inlet 14 of the solid-liquid heat exchanger E is an inlet of water before heat exchange and temperature rise and is connected with a first outlet 11 of the liquid-liquid heat exchanger D, and a second outlet 13 of the solid-liquid heat exchanger E is an outlet of water after heat exchange and temperature rise and is connected with a first inlet 12 of the liquid-liquid heat exchanger D;
a second inlet 9 of the liquid-liquid heat exchanger D is a condensed water inlet discharged by a boiler, and a second outlet 10 of the liquid-liquid heat exchanger D is a condensed water outlet after temperature rise and condensed water returns to a power plant boiler system;
an outlet 27 of the dissolving tank K is a salt solution outlet and is connected with a first inlet 28 of a coagulating sedimentation tank J, a second inlet 29 of the coagulating sedimentation tank J is a dosing port, a first outlet 50 of the coagulating sedimentation tank J is a slurry discharge port at the bottom and is connected with an inlet 31 of a filter press I, a first outlet 32 of the filter press I is a clear liquid discharge port generated after filter pressing and is connected with a third inlet 30 of the coagulating sedimentation tank J, a second outlet 33 of the filter press I is a solid discharge port generated by filter pressing, and a second outlet 47 of the coagulating sedimentation tank J is a settled salt solution discharge port and is connected with a first inlet 48 of a crystal seed precipitation device O;
a second inlet 46 of the seed crystal precipitation device O is a dosing port, a first outlet 49 of the seed crystal precipitation device O is a seed crystal particle outlet, and a second outlet 51 of the seed crystal precipitation device O is a water outlet and is connected with a first inlet 52 of the regulating tank S; the second inlet 63 of the regulating reservoir S is a hydrochloric acid inlet, the outlet 64 of the regulating reservoir S is connected with the inlet 65 of the oxidizer T, the first outlet 68 of the oxidizer T is connected with the first inlet 69 of the regulating reservoir U, the second inlet 70 of the regulating reservoir U is a sodium hydroxide inlet, the outlet 66 of the regulating reservoir U is connected with the inlet 62 of the freezing and crystallizing device R, the first outlet 53 of the freezing and crystallizing device R is connected with the first inlet 45 of the redissolution reservoir N, the second inlet 84 of the redissolution reservoir N is a condensed water inlet and is connected with the first outlet 54 of the evaporative crystallizer M, the outlet 44 of the redissolution reservoir N is connected with the first inlet 43 of the evaporative crystallizer M, and the second outlet 61 of the freezing and crystallizing device R is a high-salinity water outlet and is connected with the first inlet 71 of the evaporative crystallizer Q;
the second inlet 85 of the evaporative crystallizer M and the second inlet 86 of the evaporative crystallizer Q are steam inlets, the second outlet 55 of the evaporative crystallizer M and the first outlet 71 of the evaporative crystallizer Q are secondary steam outlets which are respectively connected with the first inlet 57 of the steam ejector X and the second inlet 58 of the steam ejector X, the third outlet 42 of the evaporative crystallizer M and the second outlet 72 of the evaporative crystallizer Q are mother liquor discharge outlets of evaporative crystallization and are both connected with the first inlet 41 of the adsorption device P, the third outlet 73 of the evaporative crystallizer Q is a crystallized salt outlet, the fourth outlet 89 of the evaporative crystallizer Q is a condensed water outlet, the third inlet 59 of the steam ejector X is a high-pressure steam inlet, and the outlet 60 of the steam ejector X is an outlet for supplying steam outside the power plant;
the second inlet 40 of the adsorption device P is a hydrochloric acid solution inlet, the first outlet 39 of the adsorption device P is a solid matter outlet containing sodium sulfate, the first inlet 37 of the desorption device L is connected with the first inlet 37 of the desorption device L, the second inlet 34 of the desorption device L is a sodium hydroxide inlet, the first outlet 88 of the desorption device L is an adsorbent outlet, the third inlet 77 of the adsorption device P is connected with the second outlet 36 of the desorption device L, the second outlet 36 of the desorption device L is a sodium sulfate solution outlet after desorption and is connected with the third inlet 38 of the evaporation crystallizer M, the second outlet 35 of the adsorption device P is a solution outlet after adsorption and is connected with the second inlet 75 of the refrigeration device V, the first outlet 78 of the refrigeration device V is a crystal salt discharge port, the second outlet 79 of the refrigeration device V is connected with the first inlet 80 of the evaporation crystallizer W, the first outlet 82 of the evaporation crystallizer W is a crystal salt outlet, the second outlet 81 of the evaporation crystallizer W is a mother liquor outlet of the evaporation crystallization, and is connected with the third inlet 76 of the refrigerating device V, the third outlet 87 of the evaporative crystallizer W is a mother liquor discharge outlet of evaporative crystallization, and the fourth outlet 83 of the evaporative crystallizer W is a condensed water discharge outlet.
The dryer A adopts one of an electric heating rotary kiln, an electric heating rake furnace and an electric heating roller dryer A.
And the solid-liquid heat exchanger E adopts a water-cooled drum-type slag cooler or a disc-type slag cooler.
The liquid-liquid heat exchanger D adopts a plate type or tube type heat exchanger.
A method for recycling waste salt based on the system as claimed in any one of claims 1 to 4, which comprises the following processes:
sending the waste salt into a dryer A for drying, wherein the drying temperature in the dryer A is controlled to be between 100 ℃ and 300 ℃, the dryer A adopts a vacuum drying mode, the internal negative pressure is in a state, and the vacuum degree is between 0.008MPa and 0.01 MPa;
the dry tail gas generated by the dryer A is treated by the dust and deacidification device B, the specific process is that the dust and deacidification device B adopts a high-temperature resistant composite filter drum type dust remover, a filter element of the high-temperature resistant composite filter drum type dust remover adopts an inorganic silicate composite material, a vanadium-titanium catalyst is arranged in a drum core of the high-temperature resistant composite filter drum type dust remover, and the vanadium-titanium catalyst is used as one of desulfurization and denitrification catalysts to reduce nitrogen oxides in the dry tail gas into nitrogen.
The dust-removing deacidification device B removes acid gases such as hydrogen chloride, sulfide gas, hydrogen fluoride gas and the like in the flue gas by adding an alkaline agent, wherein the alkaline agent is sodium hydroxide, sodium carbonate or calcium hydroxide, the operable temperature of the dust-removing deacidification device B is 30-600 ℃, the gas treated by the dust-removing deacidification device B is driven by a vacuum device C, and the deacidified gas enters a power plant boiler through an induced draft fan Z to be burnt;
the dried waste salt enters a high-temperature pyrolyzer F, the dried waste salt is pyrolyzed, the high-temperature pyrolyzer F is pyrolyzed in an oxygen-free state, the pyrolysis temperature of the high-temperature pyrolyzer F is controlled to be 300-600 ℃, the instantaneous highest temperature is not more than 1000 ℃, a continuous feeding and continuous discharging production mode is adopted, pyrolysis gas generated by the high-temperature pyrolyzer F enters a dust and acid remover H through a negative pressure fan G for dust and acid removal, and the gas treated by the dust and acid remover H enters a power plant boiler;
the dust and deacidification device H adopts a high-temperature resistant composite filter drum type dust remover, a filter element of the high-temperature resistant composite filter drum type dust remover adopts an inorganic silicate composite material, a drum core of the high-temperature resistant composite filter drum type dust remover is internally provided with a vanadium-titanium catalyst, and the vanadium-titanium catalyst is used as one of desulfurization and denitrification catalysts to reduce nitrogen oxides in dry tail gas into nitrogen.
The acid gas content of the outlets of the dedusting deacidification device B and the dedusting deacidification device H is lower than 5 milligram liters, and the dust content of the outlets of the dedusting deacidification device B and the dedusting deacidification device H is lower than 3 milligram liters.
Solid waste generated by the dust and acid remover B and the dust and acid remover H is sodium sulfate, sodium chloride, sodium fluoride, or a mixture containing a small amount of sodium nitrate, part of dust, or a mixture of calcium salts, and the like, waste salt generated by pyrolysis along with the high-temperature pyrolyzer F enters the solid-liquid heat exchanger E to exchange heat with water from the liquid-liquid heat exchanger D, the waste salt after heat exchange and temperature reduction enters the dissolving tank K to be dissolved, the water after heat exchange and temperature rise enters the liquid-liquid heat exchanger D and exchanges heat with condensed water from a power plant boiler in the liquid-liquid heat exchanger D, the condensed water after heat exchange and temperature rise returns to a boiler system, and high-temperature heat in the waste salt is recycled into the boiler;
the temperature of the salt at the inlet of the solid-liquid heat exchanger E is lower than 700 ℃, and the temperature of the salt at the outlet of the solid-liquid heat exchanger E is lower than 100 ℃.
The temperature of the condensed water entering the boiler by the liquid-liquid heat exchanger D is lower than 100 ℃, and the temperature of the water at the outlet is lower than 100 ℃.
Dangerous waste salt from the solid-liquid heat exchanger E enters a dissolving tank K, salt solution in the dissolving tank K enters a coagulating sedimentation tank J, the salt solution reacts with an added coagulant, a flocculating agent, a heavy metal removing agent, sodium hydroxide and the like, cations with more than two valences such as magnesium ions in the solution are combined with hydroxide radicals to generate insoluble substances, heavy metals in the solution are adsorbed and chelated, and are formed into flocculating settling and deposited at the bottom of the coagulating sedimentation tank J under the action of a coagulating medicament.
Slurry at the bottom of the coagulating sedimentation tank J enters a filter press I for filter pressing separation under the action of a slurry pump, a salt solution which is settled and clarified by the coagulating sedimentation tank J enters a crystal seed precipitation device O, calcium carbonate crystal seeds and a sodium carbonate medicament are introduced into the crystal seed precipitation device O, and the reaction of sodium carbonate and calcium ions in waste salt is realized by utilizing the principle of induced crystallization to form granular calcium carbonate;
the granular calcium carbonate is used as a desulfurizer to be reused in a power plant desulfurization system.
After the salt solution from the seed crystal precipitation device O enters a regulating tank S, adjusting ph to 5-7 in the regulating tank S by using hydrochloric acid, then entering an oxidizer T for oxidation treatment, enabling the salt solution subjected to oxidation treatment by the oxidizer T to enter a regulating tank U, adjusting the ph to more than 7 in the regulating tank U by using sodium hydroxide, and then entering a freezing crystallization device R;
the oxidizer T adopts an electrolytic oxidation mode to oxidize and decompose organic matters remained in the salt solution into carbon dioxide and water and oxidize and reduce nitrogen oxides in the salt solution into nitrogen.
Freezing and separating out sodium sulfate in the salt solution by using a freezing and crystallizing device R, feeding the obtained sodium sulfate decahydrate solid into a dissolution tank N, and feeding the solution in the dissolution tank N into an evaporation crystallizer M; carrying out evaporative crystallization to obtain anhydrous sodium sulfate, and allowing high-salinity water generated by the freezing crystallization device R to enter an evaporative crystallizer Q; evaporating and crystallizing to obtain sodium chloride, wherein the freezing temperature of the freezing and crystallizing device R is below-0 ℃, and the staying and crystallizing time of the salt solution in the freezing and crystallizing device R is more than 2 hours;
the refrigerating device V adopts a heat pump type refrigerating unit.
The adsorption device P adopts an adsorbent to adsorb sodium sulfate in the mother liquor, the adsorbent adopts zirconium hydroxide, the pH value of the solution in the adsorption device P is kept between 4 and 6, the adsorption device P discharges solid compounds formed by the reaction of the zirconium hydroxide and the sodium sulfate, the solution of the adsorption device P does not contain the sodium sulfate, solids and trace solution at the moment enters an analysis device L for analysis, the sodium sulfate solution analyzed by the analysis device L enters an evaporation crystallizer M, and the solution adsorbed by the adsorption device P enters a refrigerating device V for low-temperature refrigeration crystallization to separate out potassium chloride.
Sodium hydroxide is added into the desorption device L to realize the reduction of the desorbent, and the reduced desorbent returns to the adsorption device P again to realize the recycling of the desorbent.
The solution which is mainly composed of sodium chloride and potassium chloride and is discharged from the adsorption device P enters a refrigerating device V and then enters an evaporative crystallizer W; evaporating and crystallizing to obtain sodium chloride crystal salt, returning a mother liquor part of the evaporated and crystallized mother liquor to a refrigerating device V, discharging the other part of the evaporated and crystallized mother liquor outside, keeping the boiling point of an evaporation crystallizer W at above 11 ℃, and using the evaporation crystallizer W as a salt separator; the device adopts an FC reverse circulation evaporation crystallizer; or an Oslo evaporative crystallizer.
The invention has the following beneficial effects:
1. the method for cooperatively disposing the waste salt based on the thermal power plant is firstly provided, the technical principle of energy cascade utilization is utilized, the resource disposal of the dangerous waste salt is realized by using less energy consumption, and the purpose of greatly reducing the disposal cost of the waste salt is achieved, and the basic technical realization method is as follows: the electric energy consumed in the waste salt disposal process is taken from a power plant, and in the links of waste salt drying, waste salt pyrolysis, thermal method and cold method crystallization salt precipitation, the electric energy is converted in the form of heat energy, most of the heat energy is recovered in the power plant through heat energy recovery, secondary energy recovery is realized, or the secondary heat energy is used for industrial production, heating and the like, so that the gradient high-efficiency utilization of the energy is realized.
2. The secondary tail gas treated by waste salt is cooperatively treated by the power plant, and the efficient utilization of the secondary tail gas is realized. The technical implementation method comprises the following steps: the waste salt drying and pyrolysis adopt electric energy, so that the generated tail gas is combustible organic gas, and the heat energy of the organic tail gas is efficiently utilized and recovered by removing acid gas in the gas and feeding the residual tail gas into a power plant boiler for combustion and serving as auxiliary fuel; on the other hand, the generation condition of dioxin generated by tail gas is thoroughly avoided, so that the problem of tail gas treatment in waste salt treatment is thoroughly solved by utilizing a cooperative treatment method of a power plant.
3. The method is characterized in that high-temperature-resistant composite filter drum type dust removal, desulfurization and denitration integrated equipment is adopted for tail gas containing acidic gas generated in waste salt drying and pyrolysis process links and drying and pyrolysis process links for the first time, and simultaneously, dioxin possibly contained in the tail gas is catalyzed and completely eliminated; the method has the technical advantages of avoiding the technical defects of large heat loss of hot flue gas, deacidification high-salt wastewater generation, denitration dangerous waste generation, active carbon dangerous waste generation in an active carbon adsorption link and the like caused by the measures of rapid cooling, wet deacidification, active carbon adsorption and the like of tail gas generated by high-temperature oxidation, carbonization or waste salt melting equipment adopted in the conventional waste salt treatment, and avoiding the industrial problems that dioxin in the tail gas is not completely removed and the emission requirement is difficult to meet.
4. The electric heating drying and electric heating pyrolysis technology is adopted, on one hand, the equipment technology adopted for realizing the technology is mature and easy to realize; on the other hand is that produce high temperature flue gas with current natural gas burning and carry out the drying, carbonization, the technological means of oxidation compares, need not to set up the postcombustion room, a large amount of energy has been practiced thrift, the tail gas emission reduces more than 90%, a large amount of fine salt dirt granule have been smugglied secretly in having avoided the tail gas, the tail gas of production does not contain solid particulate matter, thereby the pipeline that has stopped current waste salt treatment equipment tail gas discharge link blocks up, the corruption, the tail gas emission is big, production control is difficult, the tail gas emission exceeds standard, fine granule is to the atmosphere emission in the tail gas, aggravate the problem of atmospheric haze.
5. Realizes 100 percent resource utilization of waste salt and hazardous waste treatment and does not generate secondary hazardous waste.
The invention has the other technical advantages of realizing 100 percent recycling of waste salt treatment, having no generation of secondary pollutant and waste residue, having no need of landfill sites, thoroughly solving the potential safety hazards of waste salt leakage and underground water pollution caused by landfill, and solving the problems of secondary dangerous waste generation and excessive solid waste amount of the existing waste salt treatment device. Compared with the prior art, the treatment of the waste salt is difficult to avoid generating secondary solid dangerous waste and needing landfill solidification treatment, and the invention realizes the treatment of soluble salt in the waste salt, such as: the method has the advantages that the sodium sulfate is recycled by 100%, the industrial-grade sodium sulfate is produced, the sodium chloride is recycled by 100%, the potassium chloride is recycled by 100%, solid insoluble substances are generated in the waste salt treatment process, and the treated solid insoluble substances can be mixed with the coal ash of the power plant to be used as building auxiliary materials, so that no secondary solid hazardous waste is generated.
6. The treatment cost is low, the lower treatment cost is realized, and the technology is easy to realize.
Because the waste salt disposal is coupled with the power plant, the energy cascade utilization and recovery technology is easier to realize, and compared with the prior art route, the technical method can obviously reduce the operation cost, solve the high energy consumption current situation of the waste salt disposal in China and reduce the carbon emission; the method consists of different process links, and the adopted technology of each process link is guaranteed by cases of successful implementation, so that the technical threshold of the implementation of the method is not high, and the method is easy to implement.
Drawings
Fig. 1 is a block diagram of a waste salt recycling system based on energy conservation and environmental protection integration of a thermal power plant according to an embodiment of the present invention.
The parts in fig. 1 are numbered and named as follows. A dryer A, a dust and acid remover B, a vacuum device C, a liquid-liquid heat exchanger D, a solid-liquid heat exchanger E, a high-temperature pyrolyzer F, a negative-pressure fan G, a dust and acid remover H, a filter press I, a dissolving tank K, a coagulating sedimentation tank J, an analytical device L, an evaporative crystallizer M, a re-dissolving tank N, a crystal seed precipitation device O, an adsorption device P, an evaporative crystallizer Q, a freezing crystallization device R, a regulating tank S, an oxidizer T, a regulating tank U, a freezing device V, an evaporative crystallizer W, a steam ejector X, a draught fan Z, a first inlet 1 of the dryer A, a first outlet 2 of the dryer A, a second outlet 3 of the dryer A, an inlet 4 of the dust remover B, a second outlet 5 of the acid remover B, a first outlet 6 of the dust and acid remover B, an inlet 7 of the vacuum device C, a noncondensable gas outlet 8 of the vacuum device C, a second inlet 9 of the liquid-liquid heat exchanger D, a high-, A second outlet 10 of the liquid-liquid heat exchanger D, a first outlet 11 of the liquid-liquid heat exchanger D, a first inlet 12 of the liquid-liquid heat exchanger D, a second outlet 13 of the solid-liquid heat exchanger E, a second inlet 14 of the solid-liquid heat exchanger E, a first outlet 15 of the solid-liquid heat exchanger E, a first inlet 16 of the solid-liquid heat exchanger E, a second outlet 17 of the high-temperature pyrolyzer F, a first inlet 18 of the high-temperature pyrolyzer F, a second inlet 19 of the high-temperature pyrolyzer F, a first outlet 20 of the high-temperature pyrolyzer F, an inlet 21 of the negative pressure fan G, an inlet 23 of the dust-removing deacidification device H, a first outlet 24 of the dust-removing deacidification device H, a second outlet 25 of the dust-removing deacidification device H, an inlet 26 of the dissolving tank K, an outlet 27 of the dissolving tank K, a first inlet 28 of the coagulating sedimentation tank J, a second inlet 29 of the coagulating sedimentation tank J, a third inlet 30 of the coagulating sedimentation tank J, an inlet 31 of the filter press, A second outlet 33 of the filter press I, a second inlet 34 of the analysis device L, a second outlet 35 of the adsorption device P, a second outlet 36 of the analysis device L, a first inlet 37 of the analysis device L, a third inlet 38 of the evaporative crystallizer M, a first outlet 39 of the adsorption device P, a second inlet 40 of the adsorption device P, a first inlet 41 of the adsorption device P, a third outlet 42 of the evaporative crystallizer M, a first inlet 43 of the evaporative crystallizer M, an outlet 44 of the redissolution pool N, a first inlet 45 of the redissolution pool N, a second inlet 46 of the seed crystal precipitation device O, a second outlet 47 of the coagulative precipitation pool J, a first inlet 48 of the seed crystal precipitation device O, a first outlet 49 of the seed crystal precipitation device O, a first outlet 50 of the coagulative precipitation pool J, a second outlet 51 of the seed crystal precipitation device O, a first inlet 52 of the adjustment pool S, a first outlet 53 of the frozen crystallization device R, a second outlet 36 of the analysis device L, a third inlet 37 of the evaporative crystallizer M, an outlet, A first outlet 54 of the evaporative crystallizer M, a second outlet 55 of the evaporative crystallizer M, a third outlet 56 of the evaporative crystallizer M, a first inlet 57 of the steam ejector X, a second inlet 58 of the steam ejector X, a third inlet 59 of the steam ejector X, an outlet 60 of the steam ejector X, a second outlet 61 of the freeze crystallizer R, an inlet 62 of the freeze crystallizer R, a second inlet 63 of the conditioning tank S, an outlet 64 of the conditioning tank S, an inlet 65 of the oxidizer T, an outlet 66 of the conditioning tank U, a first outlet 68 of the oxidizer T, a first inlet 69 of the conditioning tank U, a second inlet 70 of the conditioning tank U, a first inlet 71 of the evaporative crystallizer Q, a second outlet 72 of the evaporative crystallizer Q, a third outlet 73 of the evaporative crystallizer Q, a first outlet 74 of the evaporative crystallizer Q, a second inlet 75 of the freezing device V, a third inlet 76 of the freezing device V, a second inlet of the freezing device R, a second inlet of the conditioning tank U, a second inlet 63, A third inlet 77 of the adsorption device P, a first outlet 78 of the refrigeration device V, a second outlet 79 of the refrigeration device V, a first inlet 80 of the evaporative crystallizer W, a second outlet 81 of the evaporative crystallizer W, a first outlet 82 of the evaporative crystallizer W, a fourth outlet 83 of the evaporative crystallizer W, a second inlet 84 of the reflux pool N, a second inlet 85 of the evaporative crystallizer M, a second inlet 86 of the evaporative crystallizer Q, a third outlet 87 of the evaporative crystallizer W, a first outlet 88 of the desorption device L, a fourth outlet 89 of the evaporative crystallizer Q, a second inlet 90 of the induced draft fan Z, a first inlet 91 of the induced draft fan Z, and an outlet 92 of the induced draft fan Z.
Detailed Description
The principles and features of this invention are described below in conjunction with the following drawings, which are set forth by way of illustration only and are not intended to limit the scope of the invention.
Fig. 1 is a block diagram of a waste salt recycling system based on energy conservation and environmental protection integration of a thermal power plant according to an embodiment of the present invention, where the system includes: the device comprises a dryer A, a dust and deacidification device B, a vacuum device C, a liquid-liquid heat exchanger D, a solid-liquid heat exchanger E, a high-temperature pyrolyzer F, a negative pressure fan G, a dust and deacidification device H, a dissolving tank K, a coagulating sedimentation tank J, a filter press I, a seed crystal precipitation device O, a regulating tank S, an oxidizer T, a regulating tank U, a freezing crystallization device R, a redissolving tank N, an evaporative crystallizer M, a steam ejector X, an evaporative crystallizer Q, an analytical device L, an adsorption device P, a freezing device V, an evaporative crystallizer W and a fan Z.
Firstly, the waste salt enters a port 1 of a dryer A through a mechanical conveying device, wherein the dryer A can adopt one of an electric heating rotary kiln, an electric heating rake furnace and an electric heating roller dryer A, and the electric heating rotary kiln is preferably used. The electric heating mode can adopt a resistance type heating method or an electromagnetic type heating method, the electric heating elements are distributed at the bottom or the periphery of the kiln, and heat transfer between a heat source and materials is carried out through kiln pipes or corrosion-resistant heat transfer materials. The heating temperature in the dryer A is controlled to be between 100 ℃ and 300 ℃, and the material of the dryer A is 316L or 2205, a dual-phase steel or titanium alloy material or other corrosion-resistant materials. The negative pressure in the dryer A is in a state, and the internal vacuum degree is kept between 0.008MPa and 0.01 MPa. And the 2 port of the dryer A is a dried waste salt outlet, is connected with the 18 port of the high-temperature pyrolyzer F through a conveying pipeline and enters the high-temperature pyrolyzer F for pyrolysis.
And after the moisture content of the waste salt dried by the dryer A is lower than 0.2%, the waste salt is discharged through the port 2, enters an 18 inlet of the high-temperature pyrolyzer F through a conveying device, and enters the inside of the high-temperature pyrolyzer F for pyrolysis.
The 3 ports of the dryer A are dry tail gas outlets and are connected with the 4 ports of the dust and acid remover B, the dust and acid remover B adopts a high-temperature resistant composite filter drum type dust remover and is dry desulfurization and denitration equipment, a vanadium-titanium catalyst is arranged in a high-temperature resistant composite filter drum type drum core, the vanadium-titanium catalyst is a catalyst, the purpose of purifying acid-hydrogen gases such as sulfur dioxide, hydrogen chloride, hydrogen fluoride and the like in the gases is realized by adding an alkaline agent into the dust and acid remover B, so that the acid gases are changed into corresponding sodium salts or calcium salts, the alkaline agent is preferentially added with sodium bicarbonate, and then is limestone, sodium hydroxide and the operation temperature of the dust and acid remover B is between 30 ℃ and 600 ℃, the agent for removing nitrogen oxides is preferentially urea, and the reaction mechanism of denitration is as follows.
4NO+2NH22CO+O2---4N2+4H2O+2CO2
After the high-temperature resistant composite filter drum type dust remover purifies, the dust content of gas is lower than 5mg/m < 3 >, the removal rate of hydrogen chloride is as high as 97%, the removal rate of sulfur oxide is as high as 95%, the removal rate of nitrogen oxide is as high as 95%, and the removal rate of dioxin is as high as 99%.
Approximate reaction equation for removing dioxin:
C12HnCl8-nO2+9+0.5nO2=n-4H2O+12CO2+8-nHCl
the deacidified gas is driven by a vacuum device C, and the waste gas is discharged from an 8-port of the vacuum device C, enters a 92-port of an induced draft fan Z to be connected with an inlet of a combustion fan of a power plant under the action of the induced draft fan Z and enters a boiler to be burned.
The tail gas generated by drying the waste salt is small, and the waste salt enters a combustion-supporting air system of a power plant, is quickly diluted by the combustion-supporting air and then enters a boiler, so that the waste salt drying system is safe to operate.
The vacuum degree of the vacuum device C is maintained between 0.008MPa and 0.01 MP. The vacuum device C can adopt one or two of a Roots vacuum pump, a water ring pump, a reciprocating pump, a slide valve pump, a rotary vane pump and a diffusion pump, and a precise gas filter is arranged at a gas source inlet of the vacuum pump.
The waste salt after drying and dehydration enters a high-temperature pyrolyzer F which is an electrically heated rotary kiln; the waste salt pyrolysis and carbonization can be realized in an anaerobic state by adopting two heating modes of a resistance type or an electromagnetic type and structurally adopting a rotary type heater, a disc type heater and a high-temperature pyrolyzer F. The barrel of the high-temperature pyrolyzer F is made of corrosion-resistant 316L or 2205, corrosion-resistant materials such as dual-phase steel or titanium alloy materials and the like, a kiln lining is made of corundum composite inorganic salt corrosion-resistant materials, the optimal control point of the pyrolysis temperature of the high-temperature pyrolyzer F is 300-600 ℃, the instantaneous highest temperature is not more than 1000 ℃, the high-temperature pyrolyzer F adopts a continuous feeding and continuous discharging operation mode, and under the condition of high temperature and oxygen deficiency of organic matters in waste salt, molecular chains of macromolecular organic matters are opened at high temperature to become organic compounds based on hydrocarbon oxygen nitrogen, sulfur-containing elements or chlorine-containing elements in organic micromolecule gaseous state, and acid gases such as hydrogen fluoride, hydrogen chloride and the like can also be contained, and part of carbon elements in the waste salt exist in the form of carbon ash. The cracking temperature of the high-temperature pyrolyzer F can be smoothly adjusted and is not more than 900 ℃ at most. The electric heating cracking furnace has the advantages of small furnace body, high efficiency and no secondary dust generation. Pyrolysis gas generated by the high-temperature pyrolyzer F is discharged from a port F20 of the high-temperature pyrolyzer and enters a 21 inlet of a negative pressure fan G, the negative pressure fan G is a high-temperature-resistant corrosion-resistant fan, the gas can be subjected to rated high temperature resistance of 600 ℃, the gas enters a dust-removing deacidification device H under the action of fan supercharging pressure, the dust-removing deacidification device H adopts a high-temperature-resistant composite filter cartridge type dust remover, the mechanism of the dust-removing deacidification device H is the same as that of the dust-removing deacidification device B, and after the hydrogen fluoride, hydrogen chloride, hydrogen sulfide, sulfur dioxide, nitrogen oxide gas and the like which may be contained in the gas are.
The high-temperature gas after deacidification and dedusting enters an inlet Z of a draught fan after passing through a 25-port outlet of a dedusting deacidification device H, enters the boiler to be burnt, and simultaneously the waste heat of the gas is recycled. Solid waste generated by the dedusting and deacidifying device H and the dedusting and deacidifying device B, such as: sodium sulfate, sodium sulfide, sodium chloride or corresponding calcium salt and the like enter the port 19 of the high-temperature pyrolyzer F from the port 5 and the port 24 respectively, and enter the solid-liquid heat exchanger E along with waste salt.
More than 90% of organic matters in the waste salt after pyrolysis are removed, macromolecular organic matters in the waste salt are split, the cost of the macromolecular organic matters is small, the toxicity of the organic matters is eliminated, the hot waste salt enters the solid-liquid heat exchanger E, hot salt enters the port 16 of the solid-liquid heat exchanger EE, the salt after cooling exits from the port 15, low-temperature water enters the port 14 of the solid-liquid heat exchanger EE, and high-temperature water exits from the port 13 of the solid-liquid heat exchanger EE. The water temperature of the inlet 14 of the solid-liquid heat exchanger E is between 37 and 70 ℃ and the water temperature of the outlet 13 is between 42 and 99 ℃, the solid-liquid heat exchanger E is a water-cooling roller type slag cooler, the temperature of the inlet waste salt is less than 600 ℃, and the temperature of the outlet salt is less than 100 ℃. The contact part of the heat exchange wall surface and the waste salt is made of corrosion-resistant 2205 dual-phase steel or titanium alloy and other corrosion-resistant materials, and the solid-liquid heat exchanger E has the advantages that the high-temperature waste salt is cooled, meanwhile, heat energy in the waste salt is recycled to a power plant boiler system, and the heat energy recovery efficiency is not lower than 80%.
The liquid-liquid heat exchanger D is a plate type or tube type heat exchanger, wherein condensed water of a boiler system enters from an inlet 9, the temperature of the condensed water is higher than 30 ℃, and the temperature of water at an outlet 10 is higher than 42 ℃ and then returns to the boiler system. The heat exchange water forms closed internal circulation at the 11 port and the 14 port of the liquid-liquid heat exchanger D, the 12 port and the 13 port of the solid-liquid heat exchanger E and the mutually connected heat preservation pipelines to play the roles of heat carrying and heat transfer. And (3) cooling waste salt from a 15-port outlet of the solid-liquid heat exchanger E, and enabling the waste salt to pass through a conveying device and enter a dissolving tank K for dissolving, wherein the dissolving ratio of water to solid is more than 4.
Realized in the dissolving tank K that solid salt becomes liquid salt solution, the salt solution goes out from the 27 mouths of dissolving tank K, get into the pipeline entering pond that 28 mouths of coagulating sedimentation pond J are connected, 29 mouths of coagulating sedimentation pond J are for adding the medicine mouth, add and coagulate the medicament, the heavy metal remover, sodium hydroxide etc. through the medicament reaction, effectively get rid of the magnesium ion in the coagulating sedimentation pond J, multivalent cations such as iron ion, and heavy metal ion, suspension insoluble etc. the coagulating sedimentation pond J adopts the integration depositing reservoir.
The settling time of the coagulating sedimentation tank J is not less than 120 minutes, slurry at the bottom of the coagulating sedimentation tank J enters a port 31 of the filter press I through a port 50, after the water content of solid is reduced to below 50% through filter pressing separation, the slurry is discharged from a port 33 to enter waste coal cinder and coal ash of a power plant as building auxiliary materials, and clear liquid returns to a port 30 of the coagulating sedimentation tank J through a port 32 of the filter press I.
The filter press I adopts a plate-and-frame filter press, and consists of five parts, namely a filter plate of the filter press, a hydraulic system, a filter press frame, a filter plate transmission system, an electrical system and the like. The plate-and-frame filter press has mature technology and is generally applied, and is necessary equipment in the field of sewage treatment.
The salt solution after precipitation and clarification enters a crystal seed precipitation device O which is a crystallization reaction tank for precipitating calcium carbonate crystals. Calcium carbonate seed crystals and sodium carbonate medicaments are introduced into a port 46 of the seed crystal precipitation device O, the reaction of sodium carbonate and calcium ions is realized by utilizing the principle of induced crystallization, calcium carbonate fine particles are generated, the fine particles are repeatedly circulated in a salt solution through the seed crystal precipitation device O, the fine calcium carbonate is gradually attached to the surface of the calcium carbonate seed crystals and gradually grows up to form granular calcium carbonate, the calcium carbonate particles with certain particle size are discharged through a port 49 of the seed crystal precipitation device O, and the calcium carbonate particles are dehydrated and used as a desulfurizing agent of a thermal power plant. The depth of the seed crystal precipitation device O is more than 5 times of the flow velocity of the saline solution, the width of the seed crystal precipitation device O is more than 4 times of the flow velocity of the saline solution, and the volume of the device is more than 10 times. The calcium carbonate induced crystallization technology is mature, realizes resource recovery and utilization of calcium ions in salt, is used for a power plant desulfurization system, and is used as a desulfurizer. The decalcification rate of the seed crystal precipitation device OO reaches more than 80 percent.
And the effluent of the seed crystal precipitation device O is discharged from a port 51 and enters an adjusting tank s, the adjusting tank s is a tank body with a civil structure, the anticorrosion design is adopted, hydrochloric acid enters from a port 63 of the adjusting tank, and the ph is adjusted to be between 5 and 7. The effluent of the regulating reservoir s enters an oxidizer T which is characterized by generating hydroxyl radical "OH" with strong oxidizing power, the free radical forming time of the oxidizer T is 10-14 s, and the reaction time of the free radical is about 1 s; the reaction time of the free radical and other organic matters is 1-10s, and the oxidation rate constant is 106-109L/mol.s; the diffusion rate limit is 1010L/mol. s. The oxidizer T reduces the organic matter residue in the salt solution to below 2ppm and the total nitrogen to below 10 ppm.
And (3) after the effluent of the oxidizer T is regulated by a regulating reservoir U, adding sodium hydroxide to enable the salt solution ph to be more than 7, and then enabling the effluent to enter a freezing crystallization device R. And the freezing and crystallizing device R realizes freezing and precipitation of sodium sulfate in the salt solution, the freezing temperature of the freezing and crystallizing device R is below 0 ℃ below zero, and sodium sulfate decahydrate is produced. The freezing and crystallizing device R consists of a heat pump type refrigerator, a precooler, a freezer, a crystallizer, a settler and the like. The condenser in the heat pump type refrigerating machine cooling system combines water cooling and air cooling, the inlet water of the condenser is the supplementary deionized water of a boiler of a thermal power plant, the water temperature is normal temperature, the water temperature is increased after heat exchange and enters a water replenishing system of the boiler of the power plant, the heat exchange temperature difference is not less than 2 ℃, the air cooling part is cooled by combustion-supporting air of the power plant, the combustion-supporting air enters the boiler after heat exchange, the air cooling heat exchanger adopts a dividing wall type heat exchanger, the heat exchange temperature difference is not less than 2 ℃, the water temperature and the air temperature entering the boiler are improved through the water cooling and the air cooling of the condenser in the refrigerating machine cooling system, the waste heat generated by the refrigerating machine is recycled to the boiler system, and the heat energy recovery efficiency is more. The salt solution of the freezing and crystallizing device R stays for crystallization time longer than 2 hours.
Sodium sulfate decahydrate separated out by the freezing crystallization device R enters a re-dissolving tank N, and the re-dissolving water adopts condensed water of the evaporative crystallizer M. Condensed water enters the dissolution tank N from the outlet 54 of the evaporative crystallizer M and the outlet 84 of the evaporative crystallizer M.
The evaporative crystallizer M adopts a reverse circulation FC or Oslo-based crystallizer to realize the production of anhydrous sodium sulfate with large particle size. Adopting positive pressure evaporation, leading 85 ports of the evaporation liquid to enter a power plant to be saturated steam with the temperature higher than 110 ℃, leading secondary steam with the temperature of not lower than 100 ℃ to be discharged from an outlet 55, leading 42 ports of the evaporation liquid to be crystallized mother liquid, and leading the mother liquid to enter 41 ports of an adsorption device P after being connected by pipelines. And the anhydrous sodium sulfate flows out from a third outlet 56 of the evaporative crystallizer M, and the water content of the anhydrous sodium sulfate is lower than 5%. The secondary steam of 55 ports of the evaporation crystallizer M enters 57 ports of the steam ejector X and 59 ports of the steam ejector X and enters high-temperature and high-pressure steam from a boiler of a power plant, 60 ports of the steam ejector X output medium-pressure steam for supplying steam to the power plant, the steam of 60 ports can realize steam pressure and temperature according to production requirements, the steam of the power plant can be supplied externally, the steam ejector is mature in technology and is common equipment for industrial production. The liquid discharged out of the freezing and crystallizing device R is high-salinity water mainly containing sodium chloride, and the high-salinity water enters the sodium chloride evaporative crystallizer W from the port 61 and the port 71.
The evaporative crystallizer Q adopts a reverse circulation FC or Oslo-based crystallizer to realize the sodium chloride discharge with large particle size. It employs positive pressure evaporation. A86 port of the steam ejector enters saturated steam of a thermal power plant at a temperature not higher than 110 ℃, secondary steam of not lower than 100 ℃ is discharged from an 89 port, enters a 58 port of the steam ejector X, sodium chloride crystal salt is discharged from a 73 port of the steam ejector X, condensed water is discharged from a 74 port, evaporative crystallization mother liquor is discharged from a 72 port, and enters a 41 port of the adsorption device P, wherein the water content of the sodium chloride crystal salt is lower than 5%.
The adsorption device P uses an adsorbent to adsorb sodium sulfate in the mother liquor, the 41 port entering the adsorption device P is connected with the 42 port from the evaporation crystallizer M through a pipeline, the mother liquor of the evaporation crystallizer Q is saturated mother liquor, the 72 port of the mother liquor is connected with the 41 port of the adsorption device P through a pipeline, the sodium chloride and potassium chloride content in the discharged mother liquor of the evaporation crystallizer Q is more than 20 percent, the sodium sulfate content is more than 5 percent and is in a saturated state, and the solution is discharged from the 72 port and enters the 41 port of the adsorption device P, and the sodium sulfate is firstly adsorbed and separated. And a port 40 of the adsorption device P is an inlet of a hydrochloric acid solution, a port 39 of the adsorption device P is an outlet of a solid matter containing sodium sulfate, and the solid matter enters a port 37 of the analysis device L for analysis. The adsorption device P adopts zirconium hydroxide for adsorption, the pH value of the solution is kept between 4 and 6, and the basic reaction is as follows;
2ZrOOH2+Na2SO4+2HCl——[ZrOOH]2SO4+2NaCl+2H2O
[ZrOOH]2SO4is solid, after solid-liquid separation, most of water is removedInto the analysis device L.
The analyzer L reacts as follows:
[ZrOOH]2 SO4+ 2NaOH--- 2ZrOOH2+Na2SO4+2H2O
ZrOOH2the solid waste is an extremely insoluble substance, can be recycled, is almost disposable in purchase cost, has little pollution and basically does not generate solid waste. The concentration of sulfate radicals in the salt solution after the reaction is lower than 2ppm, and the adsorption is basically finished.
The resolved high-purity sodium sulfate solution returns to the 38 ports of the evaporative crystallizer M from the 36 ports of the resolving device L through a pipeline, and solid sodium sulfate is evaporated and crystallized in the evaporative crystallizer M.
The solution after adsorption by adsorption equipment P is discharged from 35 ports and enters into 75 ports of refrigerating device V, the salt solution after adsorption mainly comprises saturated sodium chloride and potassium chloride and has a small amount of other impurities, the temperature of the salt solution in refrigerating device V is reduced by below 0 ℃ due to the fact that the solubility of potassium chloride is changed along with the temperature change, potassium chloride is separated out, solid-liquid separation is achieved through a centrifugal machine of refrigerating device V, and potassium chloride crystals are discharged from 78 ports of refrigerating device V.
The refrigerating device V consists of a refrigerator, a cooling crystallizer and a solid-liquid separator, adopts a heat pump type cooling device and is mature equipment in technology. The condenser in the cooling system of the heat pump type refrigerator combines water cooling and air cooling, the inlet water of the condenser is the supplement deionized water of a boiler of a thermal power plant, the water temperature is normal temperature, the water temperature rises after heat exchange, the water enters a water supplement system of the boiler of the power plant, the heat exchange temperature difference is not less than 5 ℃, the air cooling part is cooled by combustion-supporting air of the power plant, the combustion-supporting air enters the boiler after heat exchange, wherein the air cooling heat exchanger adopts a dividing wall type heat exchanger, and the heat exchange temperature difference is not less than 5 ℃.
Sodium hydroxide enters from a 34 port of the analysis device L, the analysis agent is discharged from a 88 port of the analysis device L and enters into a 77 port of the adsorption device P, the recycling of the analysis agent is realized, and the freezing temperature of the freezing device V is lower than 0 ℃.
And a second outlet 79 of the refrigerating device V is a cold liquid outlet and enters an 80-port evaporative crystallizer W for evaporative crystallization, sodium chloride crystallized salt is discharged from an 82-port evaporative crystallization salt separator W, part of the mother liquid of the evaporative crystallization returns to a 76-port evaporative crystallizer V from an 81-port evaporative crystallization salt separator W, and part of trace mother liquid is discharged from an 83-port evaporative crystallizer W and enters a fly ash and ash residue system of a power plant to serve as a building auxiliary material.
The boiling point of the evaporative crystallizer W is kept above 11 ℃, a multi-effect evaporator or an MVR evaporative crystallizer can be adopted, the evaporative crystallizer W adopts a first-stage forced circulation evaporative crystallizer, and the type of the evaporative crystallizer W can adopt an Oslo crystallizer or a DTB type or reverse circulation FC type crystallizer.
The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the invention, and any modifications, equivalents, improvements and the like that fall within the spirit and principle of the present invention are intended to be included therein.
Claims (5)
1. The utility model provides a waste salt resource system based on energy-concerving and environment-protective integration of thermal power plant which characterized in that includes: the device comprises a dryer (A), a dust and deacidification device (B), a vacuum device (C), a liquid-liquid heat exchanger (D), a solid-liquid heat exchanger (E), a high-temperature pyrolyzer (F), a negative pressure fan (G), a dust and deacidification device (H), a dissolving tank (K), a coagulating sedimentation tank (J), a filter press (I), a seed crystal precipitation device (O), an adjusting tank (S), an oxidizer (T), an adjusting tank (U), a freezing crystallization device (R), a redissolution tank (N), an evaporating crystallizer (M), a steam ejector (X), an evaporating crystallizer (Q), a resolving device (L), an adsorption device (P), a freezing device (V), an evaporating crystallizer (W) and a draught fan (Z); the first inlet (1) of the dryer (A) is a waste salt inlet, the first outlet (2) of the dryer (A) is a dried waste salt outlet and is connected with the first inlet (18) of the high-temperature pyrolyzer (F), and the second outlet (3) of the dryer (A) is a dried tail gas outlet and is connected with the inlet (4) of the dedusting deacidifier (B); a first outlet (6) of the dust and deacidification device (B) is a waste gas outlet after dust removal and deacidification and is connected with an inlet (7) of a vacuum device (C), a second outlet (5) of the dust and deacidification device (B) and a first outlet (24) of the dust and deacidification device (H) are solid waste outlets and are connected with a second inlet (19) of the high-temperature pyrolyzer (F), a second outlet (25) of the dust and deacidification device (H) is a waste gas outlet after dust removal and deacidification and is connected with a first inlet (91) of a draught fan (Z) through a pipeline; a non-condensable gas outlet (8) of the vacuum device (C) is connected with a second inlet (90) of the induced draft fan (Z) through a pipeline, an outlet (92) of the induced draft fan (Z) is a gas outlet, and gas is introduced into a boiler of a power plant; a first outlet (20) of the high-temperature pyrolyzer (F) is a pyrolysis gas outlet and is connected with an inlet (23) of the dedusting deacidification device (H) through an inlet (21) of a negative pressure fan (G), and a second outlet (17) of the high-temperature pyrolyzer (F) is a hot waste salt outlet and is connected with a first inlet (16) of the solid-liquid heat exchanger (E); a first outlet (15) of the solid-liquid heat exchanger (E) is an outlet of cooled waste salt and is connected with an inlet (26) of the dissolving tank (K), a second inlet (14) of the solid-liquid heat exchanger (E) is an inlet of water before heat exchange and temperature rise and is connected with a first outlet (11) of the liquid-liquid heat exchanger (D), and a second outlet (13) of the solid-liquid heat exchanger (E) is an outlet of water after heat exchange and temperature rise and is connected with a first inlet (12) of the liquid-liquid heat exchanger (D); a second inlet (9) of the liquid-liquid heat exchanger (D) is a condensed water inlet discharged by the boiler, a second outlet (10) of the liquid-liquid heat exchanger (D) is a condensed water outlet after temperature rise, and the condensed water returns to the boiler system of the power plant; an outlet (27) of the dissolving tank (K) is a saline solution outlet and is connected with a first inlet (28) of a coagulating sedimentation tank (J), a second inlet (29) of the coagulating sedimentation tank (J) is a dosing port, a first outlet (50) of the coagulating sedimentation tank (J) is a mud discharge port at the bottom and is connected with an inlet (31) of a filter press (I), a first outlet (32) of the filter press (I) is a clear liquid discharge port generated after filter pressing and is connected with a third inlet (30) of the coagulating sedimentation tank (J), a second outlet (33) of the filter press (I) is a solid discharge port generated by filter pressing, and a second outlet (47) of the coagulating sedimentation tank (J) is a settled saline solution discharge port and is connected with a first inlet (48) of a crystal seed precipitation device (O); a second inlet (46) of the seed crystal precipitation device (O) is a dosing port, a first outlet (49) of the seed crystal precipitation device (O) is a seed crystal particle outlet, and a second outlet (51) of the seed crystal precipitation device (O) is a water outlet and is connected with a first inlet (52) of the regulating tank (S); the second inlet (63) of the regulating reservoir (S) is a hydrochloric acid inlet, the outlet (64) of the regulating reservoir (S) is connected with the inlet (65) of the oxidizer (T), the first outlet (68) of the oxidizer (T) is connected with the first inlet (69) of the regulating reservoir (U), the second inlet (70) of the regulating reservoir (U) is a sodium hydroxide inlet, the outlet (66) of the regulating reservoir (U) is connected with the inlet (62) of the freezing and crystallizing device (R), the first outlet (53) of the freezing and crystallizing device (R) is connected with the first inlet (45) of the dissolution reservoir (N), the second inlet (84) of the dissolution reservoir (N) is a condensed water inlet and is connected with the first outlet (54) of the evaporation crystallizer (M), the outlet (44) of the dissolution reservoir (N) is connected with the first inlet (43) of the evaporation crystallizer (M), and the second outlet (61) of the freezing and crystallizing device (R) is a high-salt water outlet, is connected with a first inlet (71) of the evaporative crystallizer (Q); a second inlet (85) of the evaporation crystallizer (M) and a second inlet (86) of the evaporation crystallizer (Q) are steam inlets, a second outlet (55) of the evaporation crystallizer (M) and a first outlet (71) of the evaporation crystallizer (Q) are secondary steam outlets which are respectively connected with a first inlet (57) of the steam ejector (X) and a second inlet (58) of the steam ejector (X), a third outlet (42) of the evaporation crystallizer (M) and a second outlet (72) of the evaporation crystallizer (Q) are mother liquor discharge outlets of evaporation crystallization and are both connected with a first inlet (41) of the adsorption device (P), a third outlet (73) of the evaporation crystallizer (Q) is a crystallized salt outlet, a fourth outlet of the evaporation crystallizer (Q) is a condensate water outlet, a third inlet (59) of the steam ejector (X) is a high-pressure steam inlet, and an outlet (60) of the steam ejector (X) is an outlet for supplying steam to an external power plant; the second inlet (40) of the adsorption device (P) is a hydrochloric acid solution inlet, the first outlet (39) of the adsorption device (P) is a solid matter outlet containing sodium sulfate, the second inlet (37) of the analysis device (L) is connected with the first inlet (37) of the analysis device (L), the second inlet (34) of the analysis device (L) is a sodium hydroxide inlet, the first outlet (88) of the analysis device (L) is an adsorbent outlet and is connected with the third inlet (77) of the adsorption device (P), the second outlet (36) of the analysis device (L) is a sodium sulfate solution outlet after analysis and is connected with the third inlet (38) of the evaporation crystallizer (M), the second outlet (35) of the adsorption device (P) is a solution outlet after adsorption and is connected with the second inlet (75) of the refrigeration device (V), the first outlet (78) of the refrigeration device (V) is a crystal salt discharge port, and the second outlet (79) of the refrigeration device (V) is connected with the first inlet (80) of the evaporation crystallizer (W), a first outlet (82) of the evaporative crystallizer (W) is a crystallized salt outlet, a second outlet (81) of the evaporative crystallizer (W) is a mother liquor outlet of evaporative crystallization and is connected with a third inlet (76) of the refrigerating device (V), a third outlet (87) of the evaporative crystallizer (W) is a mother liquor discharge outlet of the evaporative crystallization, and a fourth outlet (83) of the evaporative crystallizer (W) is a condensed water discharge outlet.
2. The energy-saving and environment-friendly integrated waste salt recycling system based on the thermal power plant as claimed in claim 1, wherein the dryer (A) is one of an electrically heated rotary kiln, an electrically heated rake furnace and an electrically heated roller dryer (A).
3. The waste salt recycling system based on the integration of energy conservation and environmental protection of the thermal power plant as claimed in claim 1, wherein the solid-liquid heat exchanger (E) adopts a water-cooled drum-type slag cooler or a disc-type slag cooler.
4. The waste salt recycling system based on the integration of energy conservation and environmental protection of the thermal power plant as claimed in claim 1, characterized in that the liquid-liquid heat exchanger (D) is a plate-type or tube-type heat exchanger.
5. A method for recycling waste salt based on the system as claimed in any one of claims 1 to 4, which comprises the following processes:
sending the waste salt into a dryer (A) for drying, wherein the drying temperature in the dryer (A) is controlled to be between 100 and 300 ℃, the dryer (A) adopts a vacuum drying mode, and the vacuum degree is between 0.008 and 0.01 MPa;
the method comprises the following steps of (1) treating dry tail gas generated by a dryer (A) through a dedusting deacidification device (B), wherein the dedusting deacidification device (B) adopts a high-temperature-resistant composite filter drum type dust remover, a filter element of the high-temperature-resistant composite filter drum type dust remover adopts an inorganic silicate composite material, a vanadium-titanium catalyst is arranged in a drum core of the high-temperature-resistant composite filter drum type dust remover, and the vanadium-titanium catalyst is used as one of desulfurization and denitrification catalysts to reduce nitrogen oxides in the dry tail gas into nitrogen;
the dust removal deacidification device (B) removes acid gases such as hydrogen chloride, sulfide gas, hydrogen fluoride gas and the like in the flue gas by adding an alkaline agent, wherein the alkaline agent is sodium hydroxide, sodium carbonate or calcium hydroxide, the operable temperature of the dust removal deacidification device (B) is 30-600 ℃, and the gas treated by the dust removal deacidification device (B) is driven by a vacuum device (C) and the deacidified gas enters a power plant boiler through a draught fan (Z) to be burnt;
the dried waste salt enters a high-temperature pyrolyzer (F) to pyrolyze the dried waste salt, the high-temperature pyrolyzer (F) is pyrolyzed in an oxygen-free state, the pyrolysis temperature of the high-temperature pyrolyzer (F) is controlled between 300 ℃ and 600 ℃, the instantaneous highest temperature is not more than 1000 ℃, a continuous feeding and continuous discharging production mode is adopted, pyrolysis gas generated by the high-temperature pyrolyzer (F) enters a dust and acid remover (H) through a negative pressure fan (G) to be subjected to dust and acid removal treatment, and gas treated by the dust and acid remover (H) enters a power plant boiler;
the dust and deacidification device (H) adopts a high-temperature resistant composite filter drum type dust remover, a filter element of the high-temperature resistant composite filter drum type dust remover adopts an inorganic silicate composite material, a drum core of the high-temperature resistant composite filter drum type dust remover is internally provided with a vanadium-titanium catalyst, and the vanadium-titanium catalyst is used as one of desulfurization and denitrification catalysts to reduce nitrogen oxides in dry tail gas into nitrogen;
the acid gas content at the outlets of the dedusting deacidification device (B) and the dedusting deacidification device (H) is lower than 5 milligram liters, and the dust content is lower than 3 milligram liters;
solid waste generated by the dedusting and deacidifying device (B) and the dedusting and deacidifying device (H) is sodium sulfate, sodium chloride, sodium fluoride or a mixture containing a small amount of sodium nitrate, part of dust or a mixture of calcium salt, etc., waste salt generated by pyrolysis along with the high-temperature pyrolyzer (F) enters a solid-liquid heat exchanger (E) to exchange heat with water from a liquid-liquid heat exchanger (D), the waste salt after heat exchange and temperature reduction enters a dissolving tank (K) to be dissolved, water after heat exchange and temperature rise enters the liquid-liquid heat exchanger (D) to exchange heat with condensed water from a power plant boiler in the liquid-liquid heat exchanger (D), the condensed water after heat exchange and temperature rise returns to a boiler system, and high-temperature heat in the waste salt is recycled into the boiler;
the temperature of the salt at the inlet of the solid-liquid heat exchanger (E) is lower than 700 ℃, and the temperature of the salt at the outlet of the solid-liquid heat exchanger (E) is lower than 100 ℃;
the temperature of the condensed water entering the boiler by the liquid-liquid heat exchanger (D) is lower than 100 ℃, and the temperature of the water at the outlet is lower than 100 ℃;
dangerous waste salt coming out of the solid-liquid heat exchanger (E) enters a dissolving tank (K), a salt solution in the dissolving tank (K) enters a coagulating sedimentation tank (J), and reacts with an added coagulant, a flocculating agent, a heavy metal remover, sodium hydroxide and the like, cations with more than two valences such as magnesium ions in the solution are combined with hydroxide radicals to generate insoluble substances, heavy metals in the solution are adsorbed and chelated, and flocculation sedimentation is formed and deposited at the bottom of the coagulating sedimentation tank (J) under the action of a coagulating medicament;
slurry at the bottom of the coagulating sedimentation tank (J) enters a filter press (I) for filter pressing separation under the action of a slurry pump, a salt solution which is settled and clarified by the coagulating sedimentation tank (J) enters a crystal seed precipitation device (O), calcium carbonate crystal seeds and a sodium carbonate medicament are introduced into the crystal seed precipitation device (O), and the reaction of sodium carbonate and calcium ions in waste salt is realized by utilizing the principle of induced crystallization to form granular calcium carbonate;
the granular calcium carbonate is used as a desulfurizer and reused in a power plant desulfurization system;
after the salt solution discharged from the seed crystal precipitation device (O) enters a regulating tank (S), ph is regulated to 5-7 in the regulating tank (S) by using hydrochloric acid, then the salt solution enters an oxidizer (T) for oxidation treatment, the salt solution subjected to oxidation treatment by the oxidizer (T) enters a regulating tank (U), ph is regulated to more than 7 in the regulating tank (U) by using sodium hydroxide, and then the salt solution enters a freezing crystallization device (R);
the oxidizer (T) adopts an electrolytic oxidation mode to oxidize and decompose organic matters remained in the salt solution into carbon dioxide and water and oxidize and reduce nitrogen oxides in the salt solution into nitrogen;
freezing and separating out sodium sulfate in the salt solution by a freezing and crystallizing device (R), feeding the obtained sodium sulfate decahydrate solid into a dissolution tank (N), and feeding the solution in the dissolution tank (N) into an evaporative crystallizer (M); carrying out evaporation crystallization to obtain anhydrous sodium sulfate, and feeding high-salt water generated by the freezing crystallization device (R) into an evaporation crystallizer (Q); evaporating and crystallizing to obtain sodium chloride, wherein the freezing temperature of the freezing and crystallizing device (R) is below 0 ℃ below zero, and the staying and crystallizing time of the salt solution in the freezing and crystallizing device (R) is more than 2 hours;
the refrigerating device (V) adopts a heat pump type refrigerating unit;
the adsorption device (P) adopts an adsorbent to adsorb sodium sulfate in the mother liquor, the adsorbent adopts zirconium hydroxide, the pH value of the solution in the adsorption device (P) is kept between 4 and 6, the adsorption device (P) discharges a solid compound formed by the reaction of the zirconium hydroxide and the sodium sulfate, the solution of the adsorption device (P) does not contain the sodium sulfate, solids and trace solution at the moment, the solution enters an analysis device (L) for analysis, the sodium sulfate solution analyzed by the analysis device (L) enters an evaporation crystallizer (M), and the solution adsorbed by the adsorption device (P) enters a refrigerating device (V) for low-temperature refrigeration crystallization to separate out potassium chloride;
sodium hydroxide is added into the desorption device (L) to realize the reduction of the desorbent, and the reduced desorbent returns to the adsorption device (P) again to realize the recycling of the desorbent;
the solution which is mainly composed of sodium chloride and potassium chloride and is discharged from the adsorption device (P) enters a refrigerating device (V) and then enters an evaporation crystallizer (W); evaporating and crystallizing to obtain sodium chloride crystal salt, returning a mother liquor part of the evaporated and crystallized mother liquor to a refrigerating device (V), discharging the other part of the evaporated and crystallized mother liquor, keeping the boiling point of an evaporation crystallizer (W) at above 11 ℃, and using the evaporation crystallizer (W) to separate the salt; the device adopts an FC reverse circulation evaporation crystallizer; or an Oslo evaporative crystallizer.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113237065A (en) * | 2021-01-13 | 2021-08-10 | 姚燕 | Intelligent control waste acid cracking furnace and waste sulfuric acid cracking process |
| CN115246649A (en) * | 2021-08-09 | 2022-10-28 | 江苏美东环境科技有限公司 | Method for preparing fertilizer-grade potassium chloride from potassium chloride organic hazardous waste salt |
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2020
- 2020-06-19 CN CN202010562203.5A patent/CN111672879A/en active Pending
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113237065A (en) * | 2021-01-13 | 2021-08-10 | 姚燕 | Intelligent control waste acid cracking furnace and waste sulfuric acid cracking process |
| CN115246649A (en) * | 2021-08-09 | 2022-10-28 | 江苏美东环境科技有限公司 | Method for preparing fertilizer-grade potassium chloride from potassium chloride organic hazardous waste salt |
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