CN111974782A - Equipment and process for treating incineration fly ash through medium-temperature thermal desorption - Google Patents
Equipment and process for treating incineration fly ash through medium-temperature thermal desorption Download PDFInfo
- Publication number
- CN111974782A CN111974782A CN202010718312.1A CN202010718312A CN111974782A CN 111974782 A CN111974782 A CN 111974782A CN 202010718312 A CN202010718312 A CN 202010718312A CN 111974782 A CN111974782 A CN 111974782A
- Authority
- CN
- China
- Prior art keywords
- thermal desorption
- sludge
- temperature thermal
- fly ash
- mud
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 238000003795 desorption Methods 0.000 title claims abstract description 57
- 239000010881 fly ash Substances 0.000 title claims abstract description 49
- 238000000034 method Methods 0.000 title claims abstract description 19
- 238000004064 recycling Methods 0.000 claims abstract description 8
- 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 claims abstract 8
- 238000005406 washing Methods 0.000 claims description 73
- 239000010802 sludge Substances 0.000 claims description 66
- 239000007788 liquid Substances 0.000 claims description 65
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 57
- 239000003546 flue gas Substances 0.000 claims description 57
- 238000002425 crystallisation Methods 0.000 claims description 38
- 230000008025 crystallization Effects 0.000 claims description 38
- 239000002918 waste heat Substances 0.000 claims description 38
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 32
- 239000004568 cement Substances 0.000 claims description 31
- 238000004523 catalytic cracking Methods 0.000 claims description 27
- 238000000926 separation method Methods 0.000 claims description 26
- 238000006243 chemical reaction Methods 0.000 claims description 23
- 229910001425 magnesium ion Inorganic materials 0.000 claims description 22
- 238000001704 evaporation Methods 0.000 claims description 19
- 230000008020 evaporation Effects 0.000 claims description 19
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 claims description 18
- 229910001424 calcium ion Inorganic materials 0.000 claims description 18
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 claims description 17
- 239000003054 catalyst Substances 0.000 claims description 17
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 claims description 16
- 239000011575 calcium Substances 0.000 claims description 16
- 239000007789 gas Substances 0.000 claims description 16
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims description 14
- 238000001914 filtration Methods 0.000 claims description 14
- 238000004140 cleaning Methods 0.000 claims description 13
- WCUXLLCKKVVCTQ-UHFFFAOYSA-M Potassium chloride Chemical compound [Cl-].[K+] WCUXLLCKKVVCTQ-UHFFFAOYSA-M 0.000 claims description 12
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical group [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 12
- 239000007787 solid Substances 0.000 claims description 12
- 239000008394 flocculating agent Substances 0.000 claims description 11
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N titanium dioxide Inorganic materials O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 claims description 9
- 238000002156 mixing Methods 0.000 claims description 7
- 239000011780 sodium chloride Substances 0.000 claims description 7
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical group Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 6
- 239000001103 potassium chloride Substances 0.000 claims description 6
- 235000011164 potassium chloride Nutrition 0.000 claims description 6
- 238000001556 precipitation Methods 0.000 claims description 6
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 6
- 239000002351 wastewater Substances 0.000 claims description 6
- GFNGCDBZVSLSFT-UHFFFAOYSA-N titanium vanadium Chemical group [Ti].[V] GFNGCDBZVSLSFT-UHFFFAOYSA-N 0.000 claims description 5
- ZFXVRMSLJDYJCH-UHFFFAOYSA-N calcium magnesium Chemical compound [Mg].[Ca] ZFXVRMSLJDYJCH-UHFFFAOYSA-N 0.000 claims description 4
- 230000001276 controlling effect Effects 0.000 claims description 4
- 239000000047 product Substances 0.000 claims description 4
- 238000005086 pumping Methods 0.000 claims description 4
- 239000006228 supernatant Substances 0.000 claims description 4
- 230000001105 regulatory effect Effects 0.000 claims description 3
- 150000003839 salts Chemical class 0.000 abstract description 14
- 231100000614 poison Toxicity 0.000 abstract description 5
- 239000002574 poison Substances 0.000 abstract description 5
- KVGZZAHHUNAVKZ-UHFFFAOYSA-N 1,4-Dioxin Chemical compound O1C=COC=C1 KVGZZAHHUNAVKZ-UHFFFAOYSA-N 0.000 description 36
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 10
- 239000000460 chlorine Substances 0.000 description 10
- 229910052801 chlorine Inorganic materials 0.000 description 10
- 229910001385 heavy metal Inorganic materials 0.000 description 7
- 239000002737 fuel gas Substances 0.000 description 6
- 239000010813 municipal solid waste Substances 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 5
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 5
- 229910052753 mercury Inorganic materials 0.000 description 5
- 239000002994 raw material Substances 0.000 description 5
- 150000001875 compounds Chemical class 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 238000012360 testing method Methods 0.000 description 4
- 238000005336 cracking Methods 0.000 description 3
- 238000004134 energy conservation Methods 0.000 description 3
- 229930195733 hydrocarbon Natural products 0.000 description 3
- 150000002430 hydrocarbons Chemical class 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 238000006116 polymerization reaction Methods 0.000 description 3
- 239000002910 solid waste Substances 0.000 description 3
- 238000007711 solidification Methods 0.000 description 3
- 230000008023 solidification Effects 0.000 description 3
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 description 2
- 239000000378 calcium silicate Substances 0.000 description 2
- 229910052918 calcium silicate Inorganic materials 0.000 description 2
- OYACROKNLOSFPA-UHFFFAOYSA-N calcium;dioxido(oxo)silane Chemical compound [Ca+2].[O-][Si]([O-])=O OYACROKNLOSFPA-UHFFFAOYSA-N 0.000 description 2
- 238000005352 clarification Methods 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 238000006703 hydration reaction Methods 0.000 description 2
- 238000005259 measurement Methods 0.000 description 2
- 230000007935 neutral effect Effects 0.000 description 2
- 238000010248 power generation Methods 0.000 description 2
- 239000002244 precipitate Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 231100000331 toxic Toxicity 0.000 description 2
- 231100000167 toxic agent Toxicity 0.000 description 2
- 230000002588 toxic effect Effects 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- 235000019738 Limestone Nutrition 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- 239000002956 ash Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000003139 buffering effect Effects 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 150000001805 chlorine compounds Chemical class 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 150000002013 dioxins Chemical class 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 231100000086 high toxicity Toxicity 0.000 description 1
- 230000036571 hydration Effects 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- 230000003472 neutralizing effect Effects 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000003825 pressing Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000005070 sampling Methods 0.000 description 1
- 239000004576 sand Substances 0.000 description 1
- 238000009270 solid waste treatment Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-N sulfuric acid group Chemical group S(O)(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 1
Images
Classifications
-
- 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
- B09B3/80—Destroying solid waste or transforming solid waste into something useful or harmless involving an extraction step
-
- 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
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8659—Removing halogens or halogen compounds
- B01D53/8662—Organic halogen compounds
-
- 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
- B09B3/40—Destroying solid waste or transforming solid waste into something useful or harmless involving thermal treatment, e.g. evaporation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
- B09B5/00—Operations not covered by a single other subclass or by a single other group in this subclass
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
- C02F11/14—Treatment of sludge; Devices therefor by de-watering, drying or thickening with addition of chemical agents
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/18—Treatment of sludge; Devices therefor by thermal conditioning
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/20—Halogens or halogen compounds
- B01D2257/206—Organic halogen compounds
- B01D2257/2064—Chlorine
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
- B09B2101/00—Type of solid waste
- B09B2101/30—Incineration ashes
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/16—Treatment of water, waste water, or sewage by heating by distillation or evaporation using waste heat from other processes
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5281—Installations for water purification using chemical agents
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
Landscapes
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Water Supply & Treatment (AREA)
- General Chemical & Material Sciences (AREA)
- Physics & Mathematics (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Thermal Sciences (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Processing Of Solid Wastes (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention discloses equipment and a process for treating incineration fly ash by intermediate-temperature thermal desorption. Not only can realize the recycling of soluble salt in the fly ash, but also can remove organic poisons such as dioxin and the like in the fly ash. The invention can realize the harmlessness, the resource utilization and the reduction of the fly ash, and the incineration fly ash is treated by utilizing the existing energy, so the treatment cost is low.
Description
Technical Field
The invention relates to the technical field of environmental protection, in particular to equipment and a process for treating incineration fly ash through intermediate-temperature thermal desorption.
Background
The household garbage incineration is the most main garbage treatment mode in China, wherein fly ash mainly comes from a waste heat utilization system and a flue gas purification system for incinerating the household garbage, is generally in a light gray powder shape and has different sizes, and the fly ash accounts for about 20% of incineration ash.
The fly ash contains heavy metal elements, dioxin and other organic substances with high toxicity, and also contains a large amount of soluble salt, so that the fly ash has great harm to the environment, is easy to pollute the environment and further harms human health. Fly ash cannot be disposed of at will and must be subjected to harmless treatment. At present, the main method is safe landfill and resource recycling after stable curing. The main treatment technologies comprise cement solidification treatment, cement kiln cooperative treatment and washing resource recovery of industrial salt.
The cement stable solidification is the most common fly ash treatment technology, and mainly the fly ash is doped into the cement, and the hydration reaction is carried out under the condition of adding water, so that hydrated calcium silicate is formed, and the hydrated calcium silicate can be solidified and contain heavy metals, thereby reducing the dissolution of the heavy metals. The technology needs a large amount of cement, occupies a large landfill space, and cannot solve the problem of pollution of organic matters such as dioxin and the like; in the cement production process, the cement hydration process can be obstructed due to the overhigh chlorine content in the fly ash, the cement quality is influenced, chloride can volatilize at the high-temperature section of the cement rotary kiln, then is condensed at a low-temperature outlet to block downstream equipment, the equipment can be stopped and washed by water, the fly ash is dissolved in water, only soluble salt in the fly ash can be recovered, and toxic organic matters such as dioxin are not treated.
Disclosure of Invention
In order to overcome the defects of the prior art, the invention aims to provide a treatment method and a process for treating incineration fly ash by intermediate-temperature thermal desorption, which can realize the recycling of soluble salt in the fly ash and remove organic poisons such as dioxin and the like in the fly ash. The invention can realize the harmlessness, the resource utilization and the reduction of the fly ash, and the incineration fly ash is treated by utilizing the existing energy, so the treatment cost is low.
The purpose of the invention is realized by adopting the following technical scheme:
an apparatus for treating incineration fly ash by intermediate temperature thermal desorption comprises a premixing device, a cleaning device, a solid-liquid separation device, a mud washing device, an intermediate temperature thermal desorption device, a dioxin catalytic cracking device, an evaporation crystallization working section, a cement treatment system and a waste heat collecting device; wherein, the evaporation crystallization section comprises a reaction tank, a filtering device and an evaporation crystallization device which are connected in sequence;
the discharge port of the premixing device is communicated with the feed port of the cleaning device, and the discharge port of the cleaning device is communicated with the feed port of the solid-liquid separation device; the liquid outlet of the solid-liquid separation device is connected with the liquid inlet of the premixing device; a mud outlet of the solid-liquid separation device is connected with a mud inlet of the mud washing device;
a conductivity meter and a calcium and magnesium ion concentration measuring instrument are arranged in the mud washing device, and soluble carbonate solution and flocculating agent are sequentially added into the mud washing device; soluble carbonate is added according to the conductivity and the concentration of calcium and magnesium ions, so that the soluble carbonate reacts with the calcium ions and the magnesium ions in the wastewater to form water-insoluble precipitate, and then a flocculating agent is added to adsorb and accelerate sludge polymerization, accelerate solution clarification and facilitate solid-liquid separation. A mud outlet of the mud washing device is connected with a mud inlet of the medium-temperature thermal desorption device, and a liquid outlet of the mud washing device is connected with a liquid inlet of the reaction tank;
sequentially adding soluble carbonate and a pH regulator into the reaction tank, wherein the pH regulator is used for regulating the pH to 7.0-7.5; according to the concentration of calcium and magnesium ions, soluble carbonate is supplemented until the solution does not produce precipitation any more, and then a pH regulator is added to make the solution from alkaline to neutral. The discharge hole of the reaction tank is connected with the feed inlet of the filtering device; the liquid outlet of the filtering device is connected with the evaporative crystallization device; a condensed water outlet of the evaporative crystallization device is connected with a water inlet of the mud washing device;
middle-temperature thermal desorption deviceProducing flue gas at 700-900 ℃; the gas outlet of the medium-temperature thermal desorption device is connected with the gas inlet of the dioxin catalytic cracking device, and the residue outlet of the medium-temperature thermal desorption device is connected with the cement treatment system; after the sludge is heated in the medium-temperature thermal desorption device, macromolecular organic matters such as dioxin in the sludge are evaporated at 700-900 ℃ into flue gas, and are partially decomposed into H2、CO、CH4And C2H6The sludge treated by the medium-temperature thermal desorption device does not contain organic matters such as dioxin, and the residues can be used as production raw materials to enter a cement treatment system to prepare finished cement.
The catalyst is added into the dioxin catalytic cracking device, the gas outlet of the dioxin catalytic cracking device is connected with the gas inlet of the waste heat collecting device, and the waste heat collecting device is connected with the evaporative crystallization device. After the flue gas treated by the medium-temperature thermal desorption device is contacted with the catalyst, toxic compounds in the flue gas are directly decomposed into micromolecular fuel gas without combustion. In particular, the fuel gas can be utilized in a waste heat utilization process, and the waste heat collecting device can be used as a heat source of the evaporative crystallization device after recovering heat energy in the fuel gas (flue gas) and can also be supplied to other devices of the invention.
Further, the mud washing device comprises a primary mud washing device, a secondary mud washing device and a tertiary mud washing device which are sequentially connected; a sludge outlet of the solid-liquid separation device is connected with a sludge inlet of the first-stage sludge washing device, and a conductivity meter and a calcium-magnesium ion concentration measuring instrument are arranged in the first-stage sludge washing device; soluble carbonate is added into the secondary sludge washing device; a flocculating agent is added into the tertiary mud washing device, a mud outlet of the tertiary mud washing device is connected with a mud inlet of the medium-temperature thermal desorption device, and a liquid outlet of the tertiary mud washing device is connected with a liquid inlet of the reaction tank.
The primary sludge washing device is mainly used for buffering and neutralizing water quality fluctuation, measuring the conductivity in a water body and detecting the concentration of calcium and magnesium ions, and specifically, the measurement of the concentration of the calcium and magnesium ions can be performed by sampling and measuring at regular intervals; according to the conductivity and the concentration of calcium and magnesium ions, sodium carbonate is added into the secondary sludge washing device to react with the calcium ions and the magnesium ions in the wastewater to form a precipitate which is insoluble in water; and a flocculating agent is added into the three-stage sludge washing device to adsorb and accelerate sludge polymerization, so that solution clarification and sludge polymerization are accelerated, and solid-liquid separation is facilitated.
Still further, the waste heat collecting device is a waste heat boiler, and a steam outlet of the waste heat boiler is also connected with a power plant. After steam generated by the waste heat of the flue gas is led to a power plant, the waste heat boiler generates power by using the steam, and the generated electric energy is applied to other devices of the invention.
Further, the flocculant is PAC and/or PAM.
Still further, the pH regulator is hydrochloric acid solution.
Further, the catalyst is a vanadium-titanium catalyst, and the vanadium-titanium catalyst is V2O5/TiO2And/or V2O5-WO3/TiO2。
Still further, still include flue gas processing system, the income gas port of flue gas processing system is connected with waste heat collection device's gas outlet.
The process of the device for treating incineration fly ash by intermediate temperature thermal desorption comprises the following steps:
1) sending the incineration fly ash into a premixing device to obtain mixed sludge, then sending the mixed sludge into a cleaning device, pumping the cleaned sludge into a solid-liquid separation device, sending wastewater in the solid-liquid separation device into the premixing device for recycling, and sending solids into a primary sludge washing device;
2) adding clear water into the primary sludge washing device, mixing the clear water with the solid to obtain turbid liquid, and measuring the conductivity and the calcium and magnesium ion concentration in the water body; then the mixture enters a secondary sludge washing device and soluble carbonate is added according to the conductivity and the concentration of calcium and magnesium ions; then the sludge enters a third-stage sludge washing device to be added with a flocculating agent, the sludge and the liquid are separated, the solid enters a medium-temperature thermal desorption device, and the liquid enters a reaction tank;
particularly, the washing and the filter pressing can be repeatedly carried out in a primary mud washing device, a secondary mud washing device and a tertiary mud washing device according to the condition of the sludge.
3) The liquid obtained in the step 2) enters a reaction tank, soluble carbonate is added to prevent the solution from generating precipitation, then a pH regulator is added to regulate the pH value to 7.0-7.5, then the liquid enters a filtering device, and supernatant is taken and introduced into an evaporative crystallization device;
4) the evaporative crystallization device obtains sodium chloride and potassium chloride products by controlling the evaporation temperature; wherein the evaporation temperature of the sodium chloride is 100 ℃, and the evaporation temperature of the potassium chloride is 55 ℃. Wherein, the condensed water generated by the evaporation crystallization device is recycled in the mud washing device.
5) Generating flue gas at 700-900 ℃ in the medium-temperature thermal desorption device, mixing the flue gas with the sludge obtained in the step 2), sending the hot flue gas into a dioxin catalytic cracking device, and sending residues into a cement treatment system; particularly, a heat source in the medium-temperature heat desorption device can recycle redundant heat energy (a household garbage treatment working section) in the anaerobic cracking working section of the solid waste, so that the aims of gradient utilization of energy and energy conservation are fulfilled.
It should be added that most of soluble chlorine elements and organic chlorides in the residue after the treatment by the medium-temperature thermal desorption device are removed, and the waste residue does not affect the normal working condition of the cement kiln and the quality of the finished cement.
6) The hot flue gas obtained in the step 3) enters a dioxin catalytic cracking device, the flue gas fully contacted with the catalyst in the dioxin catalytic cracking device is decomposed into micromolecules, hydrocarbons, chlorine and compounds thereof are removed, and the flue gas enters a waste heat collecting device;
7) the waste heat collecting device utilizes the heat energy in the flue gas to generate superheated steam, one part of the superheated steam is introduced into the evaporative crystallization device, and the other part of the superheated steam is introduced into a power plant; and the residual flue gas of the waste heat collecting device is discharged into the atmosphere after being purified by a flue gas treatment system and reaching the safe discharge standard.
Compared with the prior art, the invention has the beneficial effects that:
(1) the invention recycles soluble salt in the fly ash, and the resource is recycled, thereby realizing the resource utilization of waste; meanwhile, organic poisons such as dioxin and the like in the fly ash are effectively removed; chlorine elements in the fly ash are effectively removed, the reduction is obvious, heavy metals in the desorbed residues are effectively removed in a cement treatment system, stable solidification and other technologies are not needed, the quality of cement is not influenced, the process route is simple, and the cost is low;
(2) the waste heat collecting device recovers heat energy in the flue gas treated by the dioxin catalytic cracking device, and the heat energy can be used by each device or can be used for generating electricity by utilizing the heat energy; the medium-temperature thermal desorption device utilizes the residual heat source of the existing industrial solid waste treatment production line, reduces the production cost and saves energy.
(3) The water after the solid-liquid separation device is recycled in the premixing device, and the condensed water generated by the evaporative crystallization device is recycled in the mud washing device, so that the recycling of water resources is realized.
Drawings
FIG. 1 is a process flow diagram of the present invention.
Detailed Description
The present invention will be further described with reference to the accompanying drawings and the detailed description, and it should be noted that any combination of the embodiments or technical features described below can be used to form a new embodiment without conflict.
An apparatus for treating incineration fly ash by intermediate temperature thermal desorption, as shown in fig. 1, comprises a premixing device, a cleaning device, a solid-liquid separation device, a mud washing device, an intermediate temperature thermal desorption device, a dioxin catalytic cracking device, an evaporation crystallization section, a cement treatment system and a waste heat collecting device; wherein, the evaporation crystallization section comprises a reaction tank, a filtering device and an evaporation crystallization device which are connected in sequence;
the discharge port of the premixing device is communicated with the feed port of the cleaning device, and the discharge port of the cleaning device is communicated with the feed port of the solid-liquid separation device; the liquid outlet of the solid-liquid separation device is connected with the liquid inlet of the premixing device; a mud outlet of the solid-liquid separation device is connected with a mud inlet of the mud washing device;
the mud washing device comprises a primary mud washing device, a secondary mud washing device and a tertiary mud washing device which are sequentially connected; a sludge outlet of the solid-liquid separation device is connected with a sludge inlet of the first-stage sludge washing device, and a conductivity meter and a calcium-magnesium ion concentration measuring instrument are arranged in the first-stage sludge washing device; soluble carbonate is added into the secondary sludge washing device; a flocculating agent is added into the third-stage mud washing device, and the flocculating agent is PAC and/or PAM; a mud outlet of the third-stage mud washing device is connected with a mud inlet of the medium-temperature thermal desorption device, and a liquid outlet of the third-stage mud washing device is connected with a liquid inlet of the reaction tank;
sequentially adding soluble carbonate and a pH regulator into the reaction tank, wherein the pH regulator is used for regulating the pH to 7.0-7.5 and is a hydrochloric acid solution; according to the concentration of calcium and magnesium ions, soluble carbonate is supplemented until the solution does not produce precipitation any more, and then a pH regulator is added to make the solution from alkaline to neutral. The discharge hole of the reaction tank is connected with the feed inlet of the filtering device; the liquid outlet of the filtering device is connected with the evaporative crystallization device; a condensed water outlet of the evaporative crystallization device is connected with a water inlet of the mud washing device;
the medium-temperature thermal desorption device is used for producing flue gas at 700-900 ℃; the gas outlet of the medium-temperature thermal desorption device is connected with the gas inlet of the dioxin catalytic cracking device, and the residue outlet of the medium-temperature thermal desorption device is connected with the cement treatment system; after the sludge is heated in the medium-temperature thermal desorption device, macromolecular organic matters such as dioxin in the sludge are evaporated at 700-900 ℃ into flue gas, and are partially decomposed into H2、CO、CH4And C2H6The sludge treated by the medium-temperature thermal desorption device does not contain dioxin and other organic matters, the residues can be used as production raw materials to enter a cement treatment system to prepare finished cement, and the method comprises the following specific steps: the (residue) enters a raw material batching station → and raw materials such as sulfuric acid residue, river sand, limestone and the like sequentially enter a raw material mill → a homogenizing bank → a decomposing furnace → a rotary kiln → a clinker bank → a cement mill (which can also be directly added into the cement mill) → so as to prepare finished cement.
Adding a catalyst into a dioxin catalytic cracking device, wherein the catalyst is a vanadium-titanium catalyst which is V2O5/TiO2And/or V2O5-WO3/TiO2(ii) a The gas outlet of the dioxin catalytic cracking device is connected with the gas inlet of the waste heat collecting device, and the waste heat collecting device is respectively connected with the evaporative crystallization device and the power generation device of the power plant. After the flue gas treated by the medium-temperature thermal desorption device is contacted with the catalyst, toxic compounds in the flue gas are directly decomposed into micromolecular fuel gas without combustion.
In particular, the fuel gas can be utilized in a waste heat utilization process, the waste heat collecting device can be used as a heat source of the evaporative crystallization device after recovering heat energy in the fuel gas (flue gas), and can also be supplied to other devices of the invention, and the generated electric energy can be supplied to other devices of the invention by utilizing steam for power generation.
Example 1
The process of the device for treating incineration fly ash by intermediate temperature thermal desorption comprises the following steps:
1) sending the incineration fly ash into a premixing device to obtain mixed sludge, then sending the mixed sludge into a cleaning device, pumping the cleaned sludge into a solid-liquid separation device, sending wastewater in the solid-liquid separation device into the premixing device for recycling, and sending solids into a primary sludge washing device;
2) adding clear water into the primary sludge washing device, mixing the clear water with the solid to obtain turbid liquid, and measuring the conductivity and the calcium and magnesium ion concentration in the water body; then the mixture enters a secondary mud washing device and sodium carbonate is added according to the conductivity and the concentration of calcium and magnesium ions; feeding the sludge into a third-stage sludge washing device, adding PAM, separating sludge from liquid, feeding the solid into a medium-temperature thermal desorption device, and feeding the liquid into a reaction tank;
3) the liquid obtained in the step 2) enters a reaction tank, sodium carbonate is added to ensure that the solution does not generate precipitation any more, then a pH regulator is added to regulate the pH to 7.0, then the liquid enters a filtering device, and supernatant is taken and introduced into an evaporative crystallization device;
4) the evaporative crystallization device obtains a potassium chloride product by controlling the evaporation temperature to be 55 ℃; wherein, the condensed water generated by the evaporation crystallization device is recycled in the mud washing device.
5) Generating flue gas at 700 ℃ in the medium-temperature thermal desorption device, mixing the flue gas with the sludge obtained in the step 2), sending the hot flue gas into a dioxin catalytic cracking device, and sending residues into a cement treatment system; particularly, a heat source in the medium-temperature heat desorption device can recycle redundant heat energy (a household garbage treatment working section) in the anaerobic cracking working section of the solid waste, so that the aims of gradient utilization of energy and energy conservation are fulfilled.
6) The hot flue gas obtained in the step 3) enters a dioxin catalytic cracking device, the flue gas fully contacted with the catalyst in the dioxin catalytic cracking device is decomposed into micromolecules, hydrocarbons, chlorine and compounds thereof are removed, and the flue gas enters a waste heat collecting device;
7) the waste heat collecting device utilizes the heat energy in the flue gas to generate superheated steam, one part of the superheated steam is introduced into the evaporative crystallization device, and the other part of the superheated steam is introduced into a power plant; and the residual flue gas of the waste heat collecting device is discharged into the atmosphere after being purified by a flue gas treatment system and reaching the safe discharge standard.
Example 2
Example 1
The process of the device for treating incineration fly ash by intermediate temperature thermal desorption comprises the following steps:
1) sending the incineration fly ash into a premixing device to obtain mixed sludge, then sending the mixed sludge into a cleaning device, pumping the cleaned sludge into a solid-liquid separation device, sending wastewater in the solid-liquid separation device into the premixing device for recycling, and sending solids into a primary sludge washing device;
2) adding clear water into the primary sludge washing device, mixing the clear water with the solid to obtain turbid liquid, and measuring the conductivity and the calcium and magnesium ion concentration in the water body; then the mixture enters a secondary mud washing device and sodium carbonate is added according to the conductivity and the concentration of calcium and magnesium ions; then the sludge enters a three-stage sludge washing device to be added with PAC, sludge and liquid are separated, the solid enters a medium-temperature thermal desorption device, and the liquid enters a reaction tank;
3) the liquid obtained in the step 2) enters a reaction tank, sodium carbonate is added to ensure that the solution does not generate precipitation any more, then a pH regulator is added to regulate the pH to 7.0, then the liquid enters a filtering device, and supernatant is taken and introduced into an evaporative crystallization device;
4) the evaporative crystallization device obtains a sodium chloride product by controlling the evaporation temperature to be 100 ℃; wherein, the condensed water generated by the evaporation crystallization device is recycled in the mud washing device.
5) Generating flue gas at 900 ℃ in the medium-temperature thermal desorption device, mixing the flue gas with the sludge obtained in the step 2), sending the hot flue gas into a dioxin catalytic cracking device, and sending residues into a cement treatment system; particularly, a heat source in the medium-temperature heat desorption device can recycle redundant heat energy (a household garbage treatment working section) in the anaerobic cracking working section of the solid waste, so that the aims of gradient utilization of energy and energy conservation are fulfilled.
6) The hot flue gas obtained in the step 3) enters a dioxin catalytic cracking device, the flue gas fully contacted with the catalyst in the dioxin catalytic cracking device is decomposed into micromolecules, hydrocarbons, chlorine and compounds thereof are removed, and the flue gas enters a waste heat collecting device;
7) the waste heat collecting device utilizes the heat energy in the flue gas to generate superheated steam, one part of the superheated steam is introduced into the evaporative crystallization device, and the other part of the superheated steam is introduced into a power plant; and the residual flue gas of the waste heat collecting device is discharged into the atmosphere after being purified by a flue gas treatment system and reaching the safe discharge standard.
Performance testing
Firstly, taking the salt (potassium chloride) obtained in the step 4) and the residue obtained in the step 5) in the example 1, measuring the water content, the chlorine content, the mercury content, the lead content and the dioxin content, and obtaining the following data:
TABLE 1 salts and residues after treatment and fly ash data before treatment
| Serial number | Test items | Unit of | Fly ash before treatment | Treated salts | After treatment of the residue |
| 1 | Water content ratio | ％ | 1.84 | 1.1 | 2 |
| 2 | Chlorine | ％ | 11.3 | 62.77 | 0.88 |
| 3 | Mercury | mg/kg | 0.205 | / | 0.194 |
| 4 | Lead (II) | mg/kg | 622.5 | / | 588.4 |
| 5 | Dioxin (DIOXIN) | TEQμg/kg | 0.089 | / | / |
Secondly, the sodium chloride obtained in the step 4) of the embodiment 2 is taken for experimental test, and the following data are obtained:
TABLE 2 Property parameters of the salts obtained after treatment
| Quality index | Unit of | Standard (delicate industrial salt second level) | Actual measurement result |
| Sodium chloride | ％ | ≥97.5 | 99.65 |
| Moisture content | ％ | ≤0.8 | 0.3 |
| Water insoluble substance | ％ | ≤0.2 | / |
| Calcium magnesium ion | ％ | ≤0.6 | / |
| Sulfate ion | ％ | ≤0.9 | 0.04 |
Thirdly, taking the flue gas obtained in the step 6) of the embodiment 1 and treated by the dioxin catalytic cracking device for experimental test to obtain the following data:
TABLE 3 data of pollutants contained in flue gas treated by catalytic oxidation apparatus for dioxins
According to the data in table 1, the treated salts (potassium chloride) do not contain dioxin, lead, mercury and other heavy metal elements; the treated residue does not contain dioxin, the residual chlorine element only accounts for 0.88 percent, but the residual mercury, lead and other toxic heavy metals are also contained, which shows that the organic poisons such as dioxin and the like in the fly ash are effectively removed through the medium-temperature thermal desorption device, the chlorine element in the fly ash is also effectively removed, the reduction is obvious, and the heavy metals in the desorbed residue can be removed in a cement treatment system.
According to the data in table 2, the sodium chloride treated by the evaporation crystallization section (reaction tank, filtering device and evaporation crystallization device) meets the secondary standard of refined industrial salt, which shows that the device provided by the invention can effectively recover the industrial salt.
According to the data in table 3, the flue gas after the dioxin catalytic cracking treatment meets the standards except that the content of mercury and compounds thereof does not meet the standards, and the residual flue gas of the waste heat collecting device is discharged into the atmosphere after the residual flue gas is purified by the flue gas treatment system and reaches the safe discharge standard. The device and the process can effectively remove the content of organic poisons such as dioxin and the like.
The above embodiments are only preferred embodiments of the present invention, and the protection scope of the present invention is not limited thereby, and any insubstantial changes and substitutions made by those skilled in the art based on the present invention are within the protection scope of the present invention.
Claims (10)
1. An apparatus for treating incineration fly ash by intermediate temperature thermal desorption is characterized by comprising a premixing device, a cleaning device, a solid-liquid separation device, a mud washing device, an intermediate temperature thermal desorption device, a dioxin catalytic cracking device, an evaporation crystallization working section, a cement treatment system and a waste heat collecting device; wherein, the evaporation crystallization section comprises a reaction tank, a filtering device and an evaporation crystallization device which are connected in sequence;
the discharge port of the premixing device is communicated with the feed port of the cleaning device, and the discharge port of the cleaning device is communicated with the feed port of the solid-liquid separation device; the liquid outlet of the solid-liquid separation device is connected with the liquid inlet of the premixing device; a mud outlet of the solid-liquid separation device is connected with a mud inlet of the mud washing device;
a conductivity meter and a calcium and magnesium ion concentration measuring instrument are arranged in the mud washing device, and soluble carbonate solution and flocculating agent are sequentially added into the mud washing device; a mud outlet of the mud washing device is connected with a mud inlet of the medium-temperature thermal desorption device, and a liquid outlet of the mud washing device is connected with a liquid inlet of the reaction tank;
sequentially adding soluble carbonate and a pH regulator into the reaction tank, wherein the pH regulator is used for regulating the pH to 7.0-7.5; the discharge hole of the reaction tank is connected with the feed inlet of the filtering device; the liquid outlet of the filtering device is connected with the evaporative crystallization device; a condensed water outlet of the evaporative crystallization device is connected with a water inlet of the mud washing device;
the medium-temperature thermal desorption device is used for producing flue gas at 700-900 ℃; the gas outlet of the medium-temperature thermal desorption device is connected with the gas inlet of the dioxin catalytic cracking device, and the residue outlet of the medium-temperature thermal desorption device is connected with the cement treatment system;
the catalyst is added into the dioxin catalytic cracking device, the gas outlet of the dioxin catalytic cracking device is connected with the gas inlet of the waste heat collecting device, and the waste heat collecting device is connected with the evaporative crystallization device.
2. The equipment for treating incineration fly ash through intermediate-temperature thermal desorption according to claim 1, wherein the sludge washing device comprises a primary sludge washing device, a secondary sludge washing device and a tertiary sludge washing device which are connected in sequence; a sludge outlet of the solid-liquid separation device is connected with a sludge inlet of the first-stage sludge washing device, and a conductivity meter and a calcium-magnesium ion concentration measuring instrument are arranged in the first-stage sludge washing device; soluble carbonate is added into the secondary sludge washing device; a flocculating agent is added into the tertiary mud washing device, a mud outlet of the tertiary mud washing device is connected with a mud inlet of the medium-temperature thermal desorption device, and a liquid outlet of the tertiary mud washing device is connected with a liquid inlet of the reaction tank.
3. The apparatus for treating fly ash by mesophilic thermal desorption of claim 1, wherein the waste heat collecting device is a waste heat boiler, and the steam outlet of the waste heat boiler is further connected to a power plant.
4. The apparatus for treating incineration fly ash by mesophilic thermal desorption according to claim 1, characterized in that the flocculating agent is PAC and/or PAM.
5. The apparatus for middle temperature thermal desorption treatment of incineration fly ash according to claim 1, wherein the pH regulator is hydrochloric acid solution.
6. The apparatus for middle temperature thermal desorption treatment of incineration fly ash according to claim 1, wherein the catalyst is a vanadium-titanium catalyst, and the vanadium-titanium catalyst is V2O5/TiO2And/or V2O5-WO3/TiO2。
7. The apparatus for middle temperature thermal desorption treatment of incineration fly ash according to claim 1, wherein the soluble carbonate is sodium carbonate.
8. The apparatus for middle temperature thermal desorption treatment of incineration fly ash according to claim 1, further comprising a flue gas treatment system, wherein the gas inlet of the flue gas treatment system is connected with the gas outlet of the waste heat collecting device.
9. The process of the equipment for treating incineration fly ash by mesophilic thermal desorption according to any one of claims 1 to 8, characterized by comprising the following steps:
1) sending the incineration fly ash into a premixing device to obtain mixed sludge, then sending the mixed sludge into a cleaning device, pumping the cleaned sludge into a solid-liquid separation device, sending wastewater in the solid-liquid separation device into the premixing device for recycling, and sending solids into a sludge washing device;
2) adding clear water into the mud washing device to mix with the solid to obtain turbid liquid, measuring the electrical conductivity and the calcium and magnesium ion concentration in the water body, adding soluble carbonate according to the electrical conductivity and the calcium and magnesium ion concentration, adding a flocculating agent, separating the sludge and the liquid, allowing the solid to enter a medium-temperature thermal desorption device, and allowing the liquid to enter a reaction tank;
3) the liquid obtained in the step 2) enters a reaction tank, soluble carbonate is added until the solution does not generate precipitation any more, then a pH regulator is added to regulate the pH to 7.0-7.5, then the liquid enters a filtering device, and supernatant is taken and introduced into an evaporative crystallization device;
4) the evaporative crystallization device obtains sodium chloride and potassium chloride products by controlling the temperature;
5) generating flue gas at 700-900 ℃ in the medium-temperature thermal desorption device, mixing the flue gas with the sludge obtained in the step 2), sending the hot flue gas into a dioxin catalytic cracking device, and sending residues into a cement treatment system;
6) the hot flue gas obtained in the step 3) enters a dioxin catalytic cracking device, and the flue gas fully contacted with a catalyst in the dioxin catalytic cracking device enters a waste heat collecting device;
7) the waste heat collecting device utilizes the heat energy in the flue gas to generate superheated steam which is introduced into the evaporative crystallization device.
10. The process of the medium temperature thermal desorption equipment for treating incineration fly ash according to claim 9, wherein in the step 7), the superheated steam in the waste heat collection device is also introduced into a power plant.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010718312.1A CN111974782A (en) | 2020-07-23 | 2020-07-23 | Equipment and process for treating incineration fly ash through medium-temperature thermal desorption |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010718312.1A CN111974782A (en) | 2020-07-23 | 2020-07-23 | Equipment and process for treating incineration fly ash through medium-temperature thermal desorption |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN111974782A true CN111974782A (en) | 2020-11-24 |
Family
ID=73438978
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202010718312.1A Pending CN111974782A (en) | 2020-07-23 | 2020-07-23 | Equipment and process for treating incineration fly ash through medium-temperature thermal desorption |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN111974782A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115155279A (en) * | 2022-06-30 | 2022-10-11 | 张婷婷 | Flue gas deacidification coupling fly ash treatment method |
-
2020
- 2020-07-23 CN CN202010718312.1A patent/CN111974782A/en active Pending
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115155279A (en) * | 2022-06-30 | 2022-10-11 | 张婷婷 | Flue gas deacidification coupling fly ash treatment method |
| CN115155279B (en) * | 2022-06-30 | 2024-04-05 | 张婷婷 | Flue gas deacidification coupling fly ash treatment method |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101817650B (en) | Method for treating incinerated fly ash of domestic garbage with cooperation of cement kiln | |
| WO2009024014A1 (en) | Method for removing ammonia from coking waste water | |
| Liang et al. | Phosphorus recovery from incinerated sewage sludge ash (ISSA) and reutilization of residues for sludge pretreated by different conditioners | |
| CN112222149A (en) | Thermal desorption waste incineration fly ash treatment system and process | |
| KR20120099810A (en) | Waste to energy by way of hydrothermal decomposition and resource recycling | |
| Hlabela et al. | Barium carbonate process for sulphate and metal removal from mine water | |
| CN110937772A (en) | Method for separating organic/inorganic components from sludge | |
| CN112807874A (en) | Resource utilization system and method for hazardous waste incineration fly ash and deacidification washing water | |
| CN109293148B (en) | Treatment device and treatment method for sulfur-containing and salt-containing wastewater | |
| Li et al. | Hydrothermal treatment coupled with pyrolysis and calcination for stabilization of electroplating sludge: Speciation transformation and environmental risk of heavy metals | |
| CN112605094B (en) | Harmless treatment and green cyclic resource utilization method for high-salt-content hazardous waste | |
| CN110695059A (en) | Industrial organic waste salt treatment process | |
| Cheng et al. | An integrated process of calcium hydroxide precipitation and air stripping for pretreatment of flue gas desulfurization wastewater towards zero liquid discharge | |
| CN113292187A (en) | Resourceful treatment method and device for high-concentration ammonia nitrogen wastewater | |
| CN111744922A (en) | Fly ash treatment process in waste incineration process | |
| CN116689445A (en) | System and method for detoxication of waste incineration fly ash | |
| CN111136083A (en) | Method for recycling industrial waste miscellaneous salt | |
| CN111974782A (en) | Equipment and process for treating incineration fly ash through medium-temperature thermal desorption | |
| CN104192971A (en) | Method for treating industrial wastewater containing sulfuric acid | |
| CN117443911A (en) | Treatment method for reutilization of waste incineration fly ash | |
| CN213162409U (en) | Equipment for treating incineration fly ash through medium-temperature thermal desorption | |
| CN103013613A (en) | Clean fuelization system and fuelization method for urban sludge | |
| CN111470526A (en) | Method for producing hydrochloric acid-liquid caustic soda-composite material by using industrial waste miscellaneous salt | |
| CN102795701A (en) | Method for treating acidic waste water from titanium dioxide preparation by sulfuric acid method | |
| CN107032571B (en) | Resource treatment system and process for heavy metal sulfide sludge |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |