CN112875740A - System and method for preparing high-purity gypsum from semi-dry desulfurized fly ash - Google Patents
System and method for preparing high-purity gypsum from semi-dry desulfurized fly ash Download PDFInfo
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- 229910052602 gypsum Inorganic materials 0.000 title claims abstract description 78
- 239000010440 gypsum Substances 0.000 title claims abstract description 78
- 239000010881 fly ash Substances 0.000 title claims abstract description 37
- 238000000034 method Methods 0.000 title claims abstract description 22
- 238000005406 washing Methods 0.000 claims abstract description 115
- 239000002002 slurry Substances 0.000 claims abstract description 108
- 239000007788 liquid Substances 0.000 claims abstract description 83
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 54
- 239000003546 flue gas Substances 0.000 claims abstract description 54
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 46
- 230000023556 desulfurization Effects 0.000 claims abstract description 46
- 239000007789 gas Substances 0.000 claims abstract description 41
- 239000002956 ash Substances 0.000 claims abstract description 38
- 239000000706 filtrate Substances 0.000 claims abstract description 35
- GBAOBIBJACZTNA-UHFFFAOYSA-L calcium sulfite Chemical compound [Ca+2].[O-]S([O-])=O GBAOBIBJACZTNA-UHFFFAOYSA-L 0.000 claims abstract description 25
- 235000010261 calcium sulphite Nutrition 0.000 claims abstract description 25
- 239000000292 calcium oxide Substances 0.000 claims abstract description 24
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 claims abstract description 24
- 238000004537 pulping Methods 0.000 claims abstract description 24
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 claims abstract description 23
- 239000007921 spray Substances 0.000 claims abstract description 23
- 230000003647 oxidation Effects 0.000 claims abstract description 18
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 18
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 15
- 238000004140 cleaning Methods 0.000 claims abstract description 7
- 239000003570 air Substances 0.000 claims description 62
- 239000002245 particle Substances 0.000 claims description 27
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims description 24
- 239000000725 suspension Substances 0.000 claims description 24
- 238000005507 spraying Methods 0.000 claims description 19
- 239000000428 dust Substances 0.000 claims description 16
- 230000009471 action Effects 0.000 claims description 12
- 238000004090 dissolution Methods 0.000 claims description 10
- 239000012535 impurity Substances 0.000 claims description 8
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 7
- 239000000920 calcium hydroxide Substances 0.000 claims description 7
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims description 7
- 229910052751 metal Inorganic materials 0.000 claims description 7
- 239000002184 metal Substances 0.000 claims description 7
- 239000011148 porous material Substances 0.000 claims description 7
- 230000008569 process Effects 0.000 claims description 7
- 239000000779 smoke Substances 0.000 claims description 7
- 239000012080 ambient air Substances 0.000 claims description 6
- 230000005484 gravity Effects 0.000 claims description 6
- 238000000889 atomisation Methods 0.000 claims description 5
- 238000001035 drying Methods 0.000 claims description 4
- 238000007599 discharging Methods 0.000 claims description 3
- PASHVRUKOFIRIK-UHFFFAOYSA-L calcium sulfate dihydrate Chemical compound O.O.[Ca+2].[O-]S([O-])(=O)=O PASHVRUKOFIRIK-UHFFFAOYSA-L 0.000 claims 4
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 12
- 239000003795 chemical substances by application Substances 0.000 description 6
- 230000003009 desulfurizing effect Effects 0.000 description 6
- 238000006243 chemical reaction Methods 0.000 description 5
- 239000003054 catalyst Substances 0.000 description 4
- 239000002253 acid Substances 0.000 description 3
- 239000006227 byproduct Substances 0.000 description 3
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- 239000003513 alkali Substances 0.000 description 2
- 239000001110 calcium chloride Substances 0.000 description 2
- 229910001628 calcium chloride Inorganic materials 0.000 description 2
- 230000018044 dehydration Effects 0.000 description 2
- 238000006297 dehydration reaction Methods 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 238000005245 sintering Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000004913 activation Effects 0.000 description 1
- 238000007792 addition Methods 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000004566 building material Substances 0.000 description 1
- 229910052793 cadmium Inorganic materials 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 229910000019 calcium carbonate Inorganic materials 0.000 description 1
- WUKWITHWXAAZEY-UHFFFAOYSA-L calcium difluoride Chemical compound [F-].[F-].[Ca+2] WUKWITHWXAAZEY-UHFFFAOYSA-L 0.000 description 1
- 229910001634 calcium fluoride Inorganic materials 0.000 description 1
- 229910052804 chromium Inorganic materials 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 229910052748 manganese Inorganic materials 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 229910052750 molybdenum Inorganic materials 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 229910052710 silicon Inorganic materials 0.000 description 1
- 239000010703 silicon Substances 0.000 description 1
- 238000001694 spray drying Methods 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
- 229910052725 zinc Inorganic materials 0.000 description 1
Images
Classifications
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F11/00—Compounds of calcium, strontium, or barium
- C01F11/46—Sulfates
-
- 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
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
- B01D53/502—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific solution or suspension
-
- 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
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
- B01D53/504—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific device
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F11/00—Compounds of calcium, strontium, or barium
- C01F11/46—Sulfates
- C01F11/468—Purification of calcium sulfates
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/40—Alkaline earth metal or magnesium compounds
- B01D2251/404—Alkaline earth metal or magnesium compounds of calcium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/60—Inorganic bases or salts
- B01D2251/604—Hydroxides
-
- 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
-
- 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
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W30/00—Technologies for solid waste management
- Y02W30/50—Reuse, recycling or recovery technologies
- Y02W30/91—Use of waste materials as fillers for mortars or concrete
Abstract
The invention discloses a system and a method for preparing high-purity gypsum from semi-dry desulfurized fly ash, wherein the system comprises a washing tower, a washing pump, an oxidation fan, a gypsum pump, a dehydrator, a filtrate tank, an overflow pump, a filter press, a filtrate pump, a pulping pool, a slurry supply pump, a clean water tank and a connecting pipeline; the bottom of the washing tower is provided with a washing slurry tank, the side wall of the washing tower is provided with a flue gas inlet, and the top of the washing tower is provided with a flue gas outlet; in the washing tower, a gypsum slurry outlet, a stirrer, a washing liquid outlet, a gas distribution pipe network, a gas distribution hole plate, an overflow port, a turbulent pipe grid layer, a washing spray layer, a slurry supply spray layer, a demister layer and a demister cleaning layer are arranged from bottom to top in sequence. According to the invention, the semi-dry desulfurization ash is used as a desulfurizer of the wet desulfurization device, and the calcium oxide and the calcium sulfite in the semi-dry desulfurization ash are converted into gypsum by using the wet desulfurization system, so that the operation cost of the desulfurizer of the wet desulfurization device is reduced, and meanwhile, the harmless treatment and resource utilization of the semi-dry desulfurization ash are realized.
Description
Technical Field
The invention relates to the field of resources and environment, in particular to a system and a method for preparing high-purity gypsum from semi-dry desulfurized fly ash.
Background
Compared with a wet desulphurization process, the semi-dry process has the advantages of less investment, small occupied area, water and energy conservation and no pollution of waste water and waste acid, thereby being deeply welcomed by industries such as medium and small power plants, metallurgical sintering, heating and heat supply, chemical building materials and the like. At present, the semidry flue gas desulfurization method mainly comprises a circulating fluidized bed method (CFB), a rotary spray drying absorption method (SDA), a furnace calcium spraying tail humidifying activation method (LIFAC), a high-performance sintering waste gas purification Method (MEROS), a novel integrated desulfurization method (NID) and the like. In the operation process of the semi-dry desulfurization device, high-temperature raw flue gas carrying a large amount of dust particles is contacted with fine fog drops of atomized desulfurizer slurry, so that acid gases such as SOX, HCl and HF in the flue gas are quickly reacted with the fog drops of alkaline slurry for heat exchange to complete removal of the acid gases, and the fog drops of the desulfurizer slurry are evaporated to dryness by the flue gas and are captured by a dust remover along with the dust particles in the flue gas to form a semi-dry desulfurization byproduct, namely desulfurization ash.
The semidry desulfurization ash has complex components, contains calcium sulfite, calcium sulfate, calcium carbonate, calcium hydroxide, a small amount of calcium chloride, calcium fluoride and dust, and also contains trace heavy metals such as Zn, Cu, Cd, Mo, Cr, Mn, Ni and the like. CaSO3Is one of the main factors influencing the application of the desulfurized fly ash. How to oxidize the calcium sulfite in the desulfurized fly ash into calcium sulfate by an economic, efficient, convenient and practical method is the key for solving the application problem of the semidry desulfurized fly ash. Theoretical research on the calcium sulfite forced oxidation technology shows that a certain amount of catalyst is added to promote the conversion of calcium sulfite, the adding amount of the catalyst is about 2%, and if the adding amount of the catalyst is too small, the reaction is very slow. If no catalyst is added, the reaction is carried out at a high temperature (about 400 ℃ to 450 ℃) for 1 hour to reach an oxidation rate of more than 80%. In the view of the current research, the cost is very high whether the oxidant is added or the high-temperature treatment is carried out, and the practical application examples at home and abroad are few.
Impurities such as ash are another main factor affecting the application of desulfurized ash. The content of impurities in the desulfurized fly ash is high, and the content of compounds such as silicon, aluminum, magnesium, iron and the like can reach 50 percent. The desulfurization ash is used as a desulfurizing agent of a wet desulfurization device, impurities mixed in the desulfurization ash also enter a desulfurization system, the utilization rate of the desulfurizing agent is influenced, and particularly the quality of gypsum is influenced. How to remove the ash impurities in the desulfurization ash or the desulfurization slurry by a convenient, quick and practical mode is a key point for solving the problem of recycling the semidry desulfurization ash as a wet flue gas desulfurizer. The main source of the fly ash impurities in the desulfurization ash is smoke dust, so that the fly ash content can be reduced from the source, the dust content in the flue gas entering the semi-dry desulfurization system can be reduced, and the fly ash content in the desulfurization ash can be further reduced. In addition, in the wet desulphurization process, the fly ash content in the desulphurization slurry can be reduced by adopting an effective means, and the quality of the desulphurization gypsum is improved.
Therefore, the key to realize the resource utilization of the desulfurized fly ash is the following points: 1. must first treat the CaSO in the desulfurized fly ash3Converting into friendly and available substances. A large number of experiments prove that CaSO3Can be quickly converted into CaSO under the conditions of proper temperature, time and oxygen content4(ii) a 2. Reduce the mass ratio of original flue gas dust in the desulfurized fly ash and improve the CaSO in the desulfurized fly ash3、CaO、CaCl2The mass ratio of (a) to (b), the conversion difficulty of effective components in the desulfurized fly ash is reduced; 3. the conversion rate of useful components in the desulfurized fly ash is improved, and the additional value of resource utilization of byproducts is increased.
Disclosure of Invention
The invention provides a system and a method for preparing high-purity gypsum from semi-dry desulfurization ash, which utilize residual alkali (calcium oxide) in the semi-dry desulfurization ash as a desulfurizing agent of a wet desulfurization device, utilize a wet desulfurization system to convert calcium oxide and calcium sulfite in the semi-dry desulfurization ash into gypsum capable of being recycled, reduce the operation cost of a desulfurizing agent of the wet desulfurization device, and realize harmless treatment and recycling of the semi-dry desulfurization ash.
The technical scheme of the invention is as follows:
a system for preparing high-purity gypsum from semi-dry desulfurized fly ash comprises a washing tower, a washing pump, an oxidation fan, a gypsum pump, a dehydrator, a filtrate tank, an overflow pump, a filter press, a filtrate pump, a slurry making pool, a slurry supply pump, a clean water tank and connecting pipelines;
the bottom of the washing tower is provided with a washing slurry tank, the side wall of the washing tower is provided with a flue gas inlet, and the top of the washing tower is provided with a flue gas outlet; in the washing tower, a turbulent tube grid layer, a washing spray layer, a slurry supply spray layer, a demister layer and a demister cleaning layer are sequentially arranged between a flue gas inlet and a flue gas outlet from bottom to top; a gypsum slurry outlet, a stirrer, a washing liquid outlet, an air distribution pipe network, an air distribution hole plate and an overflow port are sequentially arranged in the washing slurry tank below the flue gas inlet from bottom to top;
the liquid inlet of the washing pump is communicated with the washing liquid outlet through a pipeline, and the liquid outlet of the washing pump is communicated with the liquid inlet of the washing spraying layer through a pipeline;
the air outlet of the oxidation fan is communicated with the air inlet of the air distribution pipe network through a pipeline;
the liquid inlet of the gypsum pump is communicated with the gypsum slurry outlet through a pipeline, and the liquid outlet of the gypsum pump is communicated with the liquid inlet of the gypsum dehydrator through a pipeline; a filtrate outlet of the gypsum dehydrator is communicated with a filtrate tank through a pipeline;
the overflow port is communicated with the overflow tank through a pipeline, and the liquid inlet of the overflow pump is communicated with the overflow tank through a pipeline; a liquid outlet of the overflow pump is communicated with a liquid inlet of the filter press through a pipeline, and a liquid outlet of the filter press is communicated with the filtrate tank through a pipeline;
the liquid inlet of the filtrate pump is communicated with the filtrate tank through a pipeline, and the liquid outlet of the filtrate pump is communicated with the liquid inlet of the pulping tank through a pipeline;
the liquid inlet of the slurry supply pump is communicated with the liquid outlet of the slurry making pool through a pipeline, and the liquid outlet of the slurry supply pump is communicated with the liquid inlet of the slurry supply spraying layer through a pipeline;
the liquid inlet of the clean water pump is communicated with the clean water tank through a pipeline, and the liquid outlet of the clean water pump is respectively communicated with the liquid inlet of the demister cleaning layer and the liquid inlet of the pulping tank through pipelines.
The invention also provides a method for preparing high-purity gypsum from semi-dry desulfurized fly ash by using the system, which comprises the following steps:
(1) conveying the semi-dry desulfurized fly ash containing a large amount of calcium sulfite-coated calcium oxide particles to a pulping tank for pulping, wherein in the pulping process, part of calcium oxide coated by calcium sulfite is dissolved to generate calcium hydroxide; the semi-dry desulfurized ash slurry subjected to preliminary dissolution is conveyed to a slurry supply spraying layer by a slurry supply pump for atomization; slurry in the washing slurry tank is pumped to the washing spray layer by a washing pump for atomization;
(2) enabling the flue gas containing sulfur dioxide and smoke dust to enter a washing tower from a flue gas inlet of the washing tower to flow upwards, sequentially passing through a turbulent tube grid layer, a washing spray layer and a slurry supply spray layer, capturing and purifying the sulfur dioxide and the smoke dust in the flue gas by atomized slurry, demisting the purified flue gas by a demister, and then discharging the demisted flue gas from a flue gas outlet of the washing tower; calcium hydroxide in the atomized slurry reacts with sulfur dioxide to generate calcium sulfite, and the calcium sulfite falls into a washing slurry tank under the action of gravity;
(3) the oxidation fan sends ambient air into the air distribution pipe network, the ambient air is evenly sent into the washing slurry pool through the air distribution holes, under the action of the air distribution hole plate, the oxidation air reacts with calcium sulfite falling into the slurry pool to generate calcium sulfate dihydrate particles (gypsum) and promote the dissolution of calcium oxide in the semi-dry desulfurization ash;
(4) under the action of gravity, calcium sulfate dihydrate particles (gypsum) with higher density and calcium oxide particles which are dissolved completely pass through the air distribution hole plate and the air distribution pipe network and enter the lower part of the washing slurry tank; impurities in the semidry desulfurization ash and fine dust in the flue gas are in a suspended state above the gas distribution pore plate to form an ash suspension layer;
(5) calcium sulfate dihydrate particles (gypsum) entering the bottom of the washing slurry tank and calcium oxide particles after dissolution are further layered under the action of a stirrer of the washing slurry tank, and the calcium sulfate dihydrate particles (gypsum) with higher density are deposited at the bottom of the washing slurry tank and continue to crystallize and grow in a suspension state to form a gypsum suspension layer; the calcium oxide particles are suspended above the gypsum suspension layer to form a desulfurizer suspension layer;
(6) slurry in the desulfurizer suspension layer is sent to the desulfurization spraying layer through a washing pump to purify sulfur dioxide in the flue gas, and the slurry in the gypsum suspension layer is sent to a dehydrator through a gypsum pump to be dehydrated to prepare high-purity gypsum; conveying the slurry of the ash suspension layer to an overflow box through an overflow port, and conveying to a filter press for dewatering and drying through an overflow pump;
(7) and the filtrate of the dehydrator and the filter press is conveyed to a filtrate box through a pipeline and is conveyed to a pulping pool through a filtrate pump for pulping.
Preferably, the distance between the gypsum slurry outlet and the bottom of the washing tower is 30-80 cm.
Preferably, the washing liquid discharge port is positioned above the stirrer and below the gas distribution pipe network; further preferably, the distance between the center of the washing liquid outlet and the lower end of the gas distribution pipe network is 50cm-150 cm.
The air distribution pipe network consists of a plurality of air distribution pipes which are horizontally arranged at equal intervals, and a plurality of air distribution holes are formed in each air distribution pipe downwards at equal intervals; one end of each gas distribution pipe is closed, and the other end of each gas distribution pipe is communicated with a main gas inlet of the gas distribution pipe network. The gas distribution pipe is preferably made of metal.
Preferably, the aperture of the air distribution holes is 10-20 mm, and the distance between adjacent air distribution holes on the same air distribution pipe is 8-25 cm; the air velocity of the perforation of the air distribution holes is 6m/s-15 m/s.
The air distribution pore plate is positioned above the air distribution pipe network and is of a porous metal plate structure. Preferably, the distance between the air distribution hole plate and the top end of the air distribution pipe network is 50cm-90 cm; the aperture ratio of the air distribution hole plate is 23-37%, and the aperture of the opening hole is 8-20 mm.
The turbulent tube grid layer is positioned above the flue gas inlet of the washing tower and below the washing spray layer and consists of at least two turbulent tube array layers; each turbulence pipe array layer is composed of a plurality of turbulence pipes which are horizontally arranged at equal intervals. The turbulent tube is preferably made of metal.
Preferably, the axial direction of the turbulence pipe is vertical to the direction of the flue gas inlet, and the pipe diameter of the turbulence pipe is 50mm-120 mm; in the same turbulent tube array layer, the distance between two adjacent turbulent tubes is 0.3-0.8 times of the diameter of the turbulent tube.
The slurry supply spraying layer is positioned above the washing spraying layer and below the demister layer and consists of a plurality of slurry distribution pipelines and slurry distribution nozzles arranged below the slurry distribution pipelines; preferably, the pressure of a liquid inlet of the slurry supply spraying layer is 0.1-0.15MPa, and the coverage rate of the nozzle is 200-350%.
Compared with the prior art, the invention has the beneficial effects that:
(1) the invention provides a solution for resource utilization of semi-dry desulfurization ash, which utilizes residual alkali (calcium oxide) in the semi-dry desulfurization ash to take the semi-dry desulfurization ash as a desulfurizing agent of a wet desulfurization device, utilizes a wet desulfurization system to convert calcium oxide and calcium sulfite in the semi-dry desulfurization ash into gypsum capable of resource utilization, reduces the running cost of a desulfurizing agent of the wet desulfurization device, and realizes harmless treatment and resource utilization of the semi-dry desulfurization ash;
(2) the invention provides a solution for improving the oxidation rate of calcium sulfite of a wet desulphurization device, wherein a turbulent tube grid layer is arranged below a washing spray layer to improve the oxidation rate of calcium sulfite in the washing desulphurization process, and a gas distribution pipe network and a gas distribution hole plate are arranged in a desulphurization slurry tank to improve the gas-liquid contact area and promote the oxidation of calcium sulfite and the dissolution of a desulfurizer;
(3) the invention provides a solution for preparing high-purity gypsum by using a wet desulphurization system, which comprises the following steps: through optimizing the structure of gas distribution pore plate and gas distribution pipe network to the stirring power of control agitator realizes that ash content, desulfurizer and the gypsum that generates carry out effective layering in the washing thick liquid pond, promotes the growth of gypsum granule, improves by-product gypsum's purity, particle size and dehydration can by a wide margin.
Drawings
FIG. 1 is a schematic structural diagram of a system for preparing high-purity gypsum from semi-dry desulfurized fly ash.
Detailed Description
The invention will be described in further detail below with reference to the drawings and examples, which are intended to facilitate the understanding of the invention without limiting it in any way.
As shown in fig. 1, the system for preparing high-purity gypsum from semi-dry desulfurized fly ash comprises a washing tower 1, a washing pump 2, an oxidation fan 3, a gypsum pump 4, a dehydrator 5, a filtrate tank 6, an overflow tank 7, an overflow pump 8, a filter press 9, a filtrate pump 10, a pulping tank 11, a pulp supply pump 12, a clean water pump 13, a clean water tank 14 and connecting pipelines.
The bottom of the washing tower 1 is a washing slurry tank, the side wall of the washing tower is provided with a flue gas inlet 101, and the top of the washing tower is provided with a flue gas outlet 102; in the washing tower 1, a turbulent tube grid layer 105, a washing spray layer 106, a slurry supply spray layer 107, a demister layer 108 and a demister cleaning layer 109 are sequentially arranged between a flue gas inlet 101 and a flue gas outlet 102 from bottom to top; the washing slurry pool below the flue gas inlet 101 is internally provided with a gypsum slurry outlet, a stirrer, a washing liquid outlet, a gas distribution pipe network 103, a gas distribution pore plate 104 and an overflow port from bottom to top in sequence.
The distance between the gypsum slurry outlet and the bottom of the washing tower 1 is 30cm-80 cm. A liquid inlet of the gypsum pump 4 is communicated with a gypsum slurry outlet through a pipeline, and a liquid outlet of the gypsum pump 4 is communicated with a liquid inlet of the gypsum dehydrator 5 through a pipeline; the filtrate outlet of the gypsum dehydrator 5 is communicated with the filtrate tank 6 through a pipeline
The washing liquid outlet is positioned above the stirrer and below the gas distribution pipe network 103; the distance between the center of the washing liquid outlet and the lower end of the gas distribution pipe network 103 is 50cm-150 cm. The liquid inlet of the washing pump 2 is communicated with the washing liquid outlet through a pipeline, and the liquid outlet of the washing pump 2 is communicated with the liquid inlet of the washing spraying layer 106 through a pipeline.
The gas distribution pipe network 103 is composed of a plurality of metal gas distribution pipes which are horizontally arranged at equal intervals, each gas distribution pipe is provided with a plurality of gas distribution holes downwards at equal intervals, the aperture of each gas distribution hole is 10-20 mm, and the interval between every two adjacent gas distribution holes on the same gas distribution pipe is 8-25 cm; the air velocity of the perforation of the air distribution holes is 6m/s-15 m/s. One end of each gas distribution pipe is closed, and the other end of each gas distribution pipe is communicated with a main gas inlet of the gas distribution pipe network 103. The air outlet of the oxidation fan 3 is communicated with the air inlet of the air distribution pipe network 103 through a pipeline.
The air distribution hole plate 104 is located above the air distribution pipe network 103, and is a porous metal plate structure. The distance between the air distribution hole plate 104 and the top end of the air distribution pipe network 103 is 50cm-90 cm; the opening rate of the air distribution hole plate 104 is 23-37%, and the opening hole diameter is 8-20 mm.
The overflow port is communicated with the overflow tank 7 through a pipeline, and the liquid inlet of the overflow pump 8 is communicated with the overflow tank 7 through a pipeline; the liquid outlet of the overflow pump 8 is communicated with the liquid inlet of the filter press 9 through a pipeline, and the liquid outlet of the filter press 9 is communicated with the filtrate tank 6 through a pipeline.
The turbulent tube grid layer 105 is positioned above the washing tower flue gas inlet 101 and below the washing spray layer 106 and consists of two turbulent tube array layers; each turbulence pipe array layer is composed of a plurality of metal turbulence pipes which are horizontally arranged at equal intervals. The axial direction of the turbulent tube is vertical to the direction of the flue gas inlet 101, and the diameter of the turbulent tube is 50mm-120 mm; in the same turbulence pipe array layer, the distance between two adjacent turbulence pipes is 0.3-0.8 times of the diameter of the turbulence pipe.
The washing spraying layer 106 has a plurality of layers, a liquid inlet of the washing pump 2 is communicated with a washing liquid outlet through a pipeline, and a liquid outlet of the washing pump 2 is communicated with a liquid inlet of the washing spraying layer 106 through a pipeline.
The slurry supply spray layer 107 is located above the washing spray layer 106. The liquid inlet of the filtrate pump 10 is communicated with the filtrate tank 6 through a pipeline, and the liquid outlet of the filtrate pump 10 is communicated with the liquid inlet of the pulping tank 11 through a pipeline. The liquid inlet of the slurry supply pump 12 is communicated with the liquid outlet of the slurry making pool 11 through a pipeline, and the liquid outlet of the slurry supply pump 12 is communicated with the liquid inlet of the slurry supply spraying layer 107 through a pipeline.
In addition, a liquid inlet of the clean water pump 13 is communicated with the clean water tank 14 through a pipeline, and a liquid outlet of the clean water pump 13 is respectively communicated with a liquid inlet of the demister cleaning layer 109 and a liquid inlet of the pulping tank 11 through pipelines.
The method for preparing the high-purity gypsum from the semi-dry desulfurized fly ash by using the system comprises the following steps:
(1) conveying the semi-dry desulfurized fly ash containing a large amount of calcium sulfite-coated calcium oxide particles to a pulping tank 11 for pulping, wherein in the pulping process, part of calcium oxide coated by calcium sulfite is dissolved to generate calcium hydroxide; the semidry desulfurized fly ash slurry subjected to preliminary dissolution is sent to a slurry supply spraying layer 107 through a slurry supply pump 12 to be atomized; slurry in the washing slurry tank is sent to a washing spray layer 106 by a washing pump 2 for atomization;
(2) enabling the flue gas containing sulfur dioxide and smoke dust to enter the washing tower 1 from a flue gas inlet 101 of the washing tower 1 to flow upwards, sequentially passing through a turbulent tube grid layer 105, a washing spray layer 106 and a slurry supply spray layer 107, capturing and purifying the sulfur dioxide and smoke dust in the flue gas by atomized slurry, demisting the purified flue gas by a demister, and then discharging the flue gas from a flue gas outlet 102 of the washing tower 1; calcium hydroxide in the atomized slurry reacts with sulfur dioxide to generate calcium sulfite, and the calcium sulfite falls into a washing slurry tank under the action of gravity;
(3) the oxidation fan 3 sends ambient air into the gas distribution pipe network 103, the ambient air is evenly sent into the washing slurry tank through the gas distribution holes, under the action of the gas distribution hole plate 104, the oxidation air reacts with calcium sulfite falling into the slurry tank to generate calcium sulfate dihydrate particles (gypsum) and promote the dissolution of calcium oxide in the semi-dry desulfurization ash;
(4) under the action of gravity, calcium sulfate dihydrate particles (gypsum) with higher density and calcium oxide particles which are dissolved completely pass through the air distribution hole plate 104 and the air distribution pipe network 103 and enter the lower part of the washing slurry tank; impurities in the semidry desulfurization ash and fine dust in the flue gas are in a suspended state above the gas distribution pore plate 104 to form an ash suspension layer;
(5) calcium sulfate dihydrate particles (gypsum) entering the bottom of the washing slurry tank and calcium oxide particles after dissolution are further layered under the action of a stirrer of the washing slurry tank, and the calcium sulfate dihydrate particles (gypsum) with higher density are deposited at the bottom of the washing slurry tank and continue to crystallize and grow in a suspension state to form a gypsum suspension layer; the calcium oxide particles are suspended above the gypsum suspension layer to form a desulfurizer suspension layer;
(6) the slurry in the desulfurizer suspension layer is sent to the desulfurization spray layer through the washing pump 2 to purify sulfur dioxide in the flue gas, and the slurry in the gypsum suspension layer is sent to the dehydrator 5 through the gypsum pump 4 to be dehydrated to prepare high-purity gypsum; the slurry of the ash suspension layer is sent to an overflow box 7 through an overflow port and is sent to a filter press 9 through an overflow pump 8 for dehydration and drying;
(7) the filtrate from the dewatering machine 5 and the filter press 9 is sent to the filtrate tank 6 by pipelines and sent to the pulping tank 11 by the filtrate pump 10 for pulping.
The above-mentioned embodiments are intended to illustrate the technical solutions and advantages of the present invention, and it should be understood that the above-mentioned embodiments are only specific embodiments of the present invention, and are not intended to limit the present invention, and any modifications, additions, equivalents, etc. made within the scope of the principles of the present invention should be included in the scope of the present invention.
Claims (10)
1. A system for preparing high-purity gypsum from semi-dry desulfurized fly ash is characterized by comprising a washing tower, a washing pump, an oxidation fan, a gypsum pump, a dehydrator, a filtrate tank, an overflow pump, a filter press, a filtrate pump, a pulping pool, a slurry supply pump, a clean water tank and a connecting pipeline;
the bottom of the washing tower is provided with a washing slurry tank, the side wall of the washing tower is provided with a flue gas inlet, and the top of the washing tower is provided with a flue gas outlet; in the washing tower, a turbulent tube grid layer, a washing spray layer, a slurry supply spray layer, a demister layer and a demister cleaning layer are sequentially arranged between a flue gas inlet and a flue gas outlet from bottom to top; a gypsum slurry outlet, a stirrer, a washing liquid outlet, an air distribution pipe network, an air distribution hole plate and an overflow port are sequentially arranged in the washing slurry tank below the flue gas inlet from bottom to top;
the liquid inlet of the washing pump is communicated with the washing liquid outlet through a pipeline, and the liquid outlet of the washing pump is communicated with the liquid inlet of the washing spraying layer through a pipeline;
the air outlet of the oxidation fan is communicated with the air inlet of the air distribution pipe network through a pipeline;
the liquid inlet of the gypsum pump is communicated with the gypsum slurry outlet through a pipeline, and the liquid outlet of the gypsum pump is communicated with the liquid inlet of the gypsum dehydrator through a pipeline; a filtrate outlet of the gypsum dehydrator is communicated with a filtrate tank through a pipeline;
the overflow port is communicated with the overflow tank through a pipeline, and the liquid inlet of the overflow pump is communicated with the overflow tank through a pipeline; a liquid outlet of the overflow pump is communicated with a liquid inlet of the filter press through a pipeline, and a liquid outlet of the filter press is communicated with the filtrate tank through a pipeline;
the liquid inlet of the filtrate pump is communicated with the filtrate tank through a pipeline, and the liquid outlet of the filtrate pump is communicated with the liquid inlet of the pulping tank through a pipeline;
the liquid inlet of the slurry supply pump is communicated with the liquid outlet of the slurry making pool through a pipeline, and the liquid outlet of the slurry supply pump is communicated with the liquid inlet of the slurry supply spraying layer through a pipeline;
the liquid inlet of the clean water pump is communicated with the clean water tank through a pipeline, and the liquid outlet of the clean water pump is respectively communicated with the liquid inlet of the demister cleaning layer and the liquid inlet of the pulping tank through pipelines.
2. The system for preparing high-purity gypsum from semi-dry desulfurized fly ash according to claim 1, wherein the distance between the gypsum slurry outlet and the bottom of the washing tower is 30cm-80 cm.
3. The system for preparing high-purity gypsum from semi-dry desulfurized fly ash according to claim 1, wherein the distance between the center of the washing liquid outlet and the lower end of the gas distribution pipe network is 50cm-150 cm.
4. The system for preparing high-purity gypsum from semi-dry desulfurized fly ash according to claim 1, wherein said air distribution network comprises a plurality of horizontally arranged air distribution pipes arranged at equal intervals, each air distribution pipe having a plurality of air distribution holes arranged at equal intervals downward; one end of each gas distribution pipe is closed, and the other end of each gas distribution pipe is communicated with a main gas inlet of the gas distribution pipe network.
5. The system for preparing high-purity gypsum from semi-dry desulfurized fly ash according to claim 4, wherein the pore diameter of the air distribution holes is 10mm-20mm, and the distance between the adjacent air distribution holes on the same air distribution pipe is 8cm-25 cm; the air velocity of the perforation of the air distribution holes is 6m/s-15 m/s.
6. The system for preparing high-purity gypsum from semi-dry desulfurized fly ash according to claim 1, wherein said air distribution porous plate is a porous metal plate; the distance between the air distribution hole plate and the top end of the air distribution pipe network is 50cm-90 cm; the aperture ratio of the air distribution hole plate is 23-37%, and the aperture of the opening hole is 8-20 mm.
7. The system for preparing high-purity gypsum from semi-dry desulfurized fly ash according to claim 1, wherein said turbulence grid layer is composed of at least two turbulence array layers; each turbulence pipe array layer is composed of a plurality of turbulence pipes which are horizontally arranged at equal intervals.
8. The system for preparing high-purity gypsum from semi-dry desulfurized fly ash according to claim 7, wherein the turbulence pipe has an axial direction perpendicular to the direction of the flue gas inlet, and has a pipe diameter of 50mm to 120 mm; in the same turbulent tube array layer, the distance between two adjacent turbulent tubes is 0.3-0.8 times of the diameter of the turbulent tube.
9. The system for preparing high-purity gypsum from semi-dry desulfurized fly ash according to claim 1, wherein said slurry supply spraying layer comprises a plurality of slurry distribution pipes and slurry distribution nozzles installed below the slurry distribution pipes; the pressure of the liquid inlet of the slurry supply spraying layer is 0.1-0.15MPa, and the coverage rate of the nozzle is 200-350%.
10. The method for preparing high-purity gypsum from semi-dry desulfurized fly ash is characterized by comprising the following steps:
(1) conveying the semi-dry desulfurized fly ash containing a large amount of calcium sulfite-coated calcium oxide particles to a pulping tank for pulping, wherein in the pulping process, part of calcium oxide coated by calcium sulfite is dissolved to generate calcium hydroxide; the semi-dry desulfurized ash slurry subjected to preliminary dissolution is conveyed to a slurry supply spraying layer by a slurry supply pump for atomization; slurry in the washing slurry tank is pumped to the washing spray layer by a washing pump for atomization;
(2) enabling the flue gas containing sulfur dioxide and smoke dust to enter a washing tower from a flue gas inlet of the washing tower to flow upwards, sequentially passing through a turbulent tube grid layer, a washing spray layer and a slurry supply spray layer, capturing and purifying the sulfur dioxide and the smoke dust in the flue gas by atomized slurry, demisting the purified flue gas by a demister, and then discharging the demisted flue gas from a flue gas outlet of the washing tower; calcium hydroxide in the atomized slurry reacts with sulfur dioxide to generate calcium sulfite, and the calcium sulfite falls into a washing slurry tank under the action of gravity;
(3) the oxidation fan sends ambient air into the air distribution pipe network, the ambient air is evenly sent into the washing slurry pool through the air distribution holes, under the action of the air distribution hole plate, the oxidation air reacts with calcium sulfite falling into the slurry pool to generate calcium sulfate dihydrate particles and promote the dissolution of calcium oxide in the semi-dry desulfurization ash;
(4) under the action of gravity, calcium sulfate dihydrate particles with higher density and calcium oxide particles which are dissolved completely pass through the air distribution hole plate and the air distribution pipe network and enter the lower part of the washing slurry tank; impurities in the semidry desulfurization ash and fine dust in the flue gas are in a suspended state above the gas distribution pore plate to form an ash suspension layer;
(5) calcium sulfate dihydrate particles entering the bottom of the washing slurry tank and calcium oxide particles completing dissolution are further layered under the action of a stirrer of the washing slurry tank, and the calcium sulfate dihydrate particles with higher density are deposited at the bottom of the washing slurry tank and are in a suspension state to continue to crystallize and grow to form a gypsum suspension layer; the calcium oxide particles are suspended above the gypsum suspension layer to form a desulfurizer suspension layer;
(6) slurry in the desulfurizer suspension layer is sent to the desulfurization spraying layer through a washing pump to purify sulfur dioxide in the flue gas, and the slurry in the gypsum suspension layer is sent to a dehydrator through a gypsum pump to be dehydrated to prepare high-purity gypsum; conveying the slurry of the ash suspension layer to an overflow box through an overflow port, and conveying to a filter press for dewatering and drying through an overflow pump;
(7) and the filtrate of the dehydrator and the filter press is conveyed to a filtrate box through a pipeline and is conveyed to a pulping pool through a filtrate pump for pulping.
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Denomination of invention: A system and method for preparing high-purity gypsum from semi dry desulfurization ash Effective date of registration: 20230718 Granted publication date: 20230414 Pledgee: Hangzhou Gaoxin Financing Guarantee Co.,Ltd. Pledgor: HANGZHOU YUNZE ENVIRONMENTAL TECHNOLOGY Co.,Ltd. Registration number: Y2023330001516 |
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Effective date of registration: 20240108 Address after: 311215 No. 419, Shengxing Road, ningwei street, Xiaoshan District, Hangzhou City, Zhejiang Province Patentee after: Zhejiang Zeyu Technology Development Co.,Ltd. Address before: Room 605, Minghao building, 1688 Binsheng Road, Binjiang District, Hangzhou City, Zhejiang Province 310051 Patentee before: HANGZHOU YUNZE ENVIRONMENTAL TECHNOLOGY Co.,Ltd. |
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Correction item: Patentee|Address Correct: Hangzhou Yunze Environmental Technology Co., Ltd.|Room 605, Minghao building, 1688 Binsheng Road, Binjiang District, Hangzhou City, Zhejiang Province 310051 False: Zhejiang Zeyu Technology Development Co., Ltd.|311215 No. 419, Shengxing Road, ningwei street, Xiaoshan District, Hangzhou City, Zhejiang Province Number: 04-01 Volume: 40 |