CN113996142A - System and method for manufacturing zeolite and capturing carbon dioxide in flue gas by using fly ash - Google Patents
System and method for manufacturing zeolite and capturing carbon dioxide in flue gas by using fly ash Download PDFInfo
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- CN113996142A CN113996142A CN202111049652.0A CN202111049652A CN113996142A CN 113996142 A CN113996142 A CN 113996142A CN 202111049652 A CN202111049652 A CN 202111049652A CN 113996142 A CN113996142 A CN 113996142A
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- fly ash
- flue gas
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- zeolite
- carbon dioxide
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- 239000010881 fly ash Substances 0.000 title claims abstract description 183
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 179
- 239000003546 flue gas Substances 0.000 title claims abstract description 176
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 144
- 229910021536 Zeolite Inorganic materials 0.000 title claims abstract description 129
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 title claims abstract description 129
- 239000010457 zeolite Substances 0.000 title claims abstract description 129
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 77
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 72
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 27
- 238000000034 method Methods 0.000 title claims abstract description 19
- 238000001027 hydrothermal synthesis Methods 0.000 claims abstract description 75
- 238000001179 sorption measurement Methods 0.000 claims abstract description 64
- 238000001035 drying Methods 0.000 claims abstract description 52
- 238000005406 washing Methods 0.000 claims abstract description 39
- 238000001816 cooling Methods 0.000 claims abstract description 36
- 239000002253 acid Substances 0.000 claims abstract description 33
- 238000005554 pickling Methods 0.000 claims abstract description 32
- 239000003463 adsorbent Substances 0.000 claims abstract description 17
- 238000011010 flushing procedure Methods 0.000 claims abstract description 13
- 238000000926 separation method Methods 0.000 claims description 47
- 239000002956 ash Substances 0.000 claims description 29
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 27
- 230000018044 dehydration Effects 0.000 claims description 25
- 238000006297 dehydration reaction Methods 0.000 claims description 25
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 24
- 239000012024 dehydrating agents Substances 0.000 claims description 23
- 238000007599 discharging Methods 0.000 claims description 23
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 18
- 230000003009 desulfurizing effect Effects 0.000 claims description 13
- 238000004140 cleaning Methods 0.000 claims description 11
- 239000000654 additive Substances 0.000 claims description 10
- 230000000996 additive effect Effects 0.000 claims description 8
- 239000010883 coal ash Substances 0.000 claims description 8
- 239000007789 gas Substances 0.000 claims description 8
- 239000012535 impurity Substances 0.000 claims description 5
- 238000004806 packaging method and process Methods 0.000 claims description 4
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims description 3
- 229910052782 aluminium Inorganic materials 0.000 claims description 3
- 230000005484 gravity Effects 0.000 claims description 3
- 239000000463 material Substances 0.000 claims description 3
- 229910052710 silicon Inorganic materials 0.000 claims description 3
- 239000010703 silicon Substances 0.000 claims description 3
- 238000007789 sealing Methods 0.000 claims description 2
- 239000007788 liquid Substances 0.000 description 27
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 21
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 16
- 239000002699 waste material Substances 0.000 description 14
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 11
- 229910052799 carbon Inorganic materials 0.000 description 11
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 8
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 8
- 239000003513 alkali Substances 0.000 description 8
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 6
- 238000006243 chemical reaction Methods 0.000 description 6
- 238000010586 diagram Methods 0.000 description 6
- 238000010438 heat treatment Methods 0.000 description 6
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 description 4
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 4
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 239000000446 fuel Substances 0.000 description 4
- 229910052757 nitrogen Inorganic materials 0.000 description 4
- 229910052717 sulfur Inorganic materials 0.000 description 4
- 239000011593 sulfur Substances 0.000 description 4
- 239000002918 waste heat Substances 0.000 description 4
- 238000010521 absorption reaction Methods 0.000 description 3
- 238000010924 continuous production Methods 0.000 description 3
- 238000006477 desulfuration reaction Methods 0.000 description 3
- 230000023556 desulfurization Effects 0.000 description 3
- 239000000377 silicon dioxide Substances 0.000 description 3
- 238000003860 storage Methods 0.000 description 3
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 2
- 239000011324 bead Substances 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 239000011575 calcium Substances 0.000 description 2
- 229910052791 calcium Inorganic materials 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 230000007935 neutral effect Effects 0.000 description 2
- 238000012856 packing Methods 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 238000005070 sampling Methods 0.000 description 2
- 235000012239 silicon dioxide Nutrition 0.000 description 2
- 239000002893 slag Substances 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000002910 solid waste Substances 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 230000002308 calcification Effects 0.000 description 1
- 229910000019 calcium carbonate Inorganic materials 0.000 description 1
- 239000004568 cement Substances 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 229910052593 corundum Inorganic materials 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 238000007667 floating Methods 0.000 description 1
- 238000000227 grinding Methods 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 230000009919 sequestration Effects 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 238000002791 soaking Methods 0.000 description 1
- 239000011343 solid material Substances 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- LSNNMFCWUKXFEE-UHFFFAOYSA-L sulfite Chemical class [O-]S([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-L 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
- 229910001845 yogo sapphire Inorganic materials 0.000 description 1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
-
- 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
- B01D53/26—Drying gases or vapours
- B01D53/265—Drying gases or vapours by refrigeration (condensation)
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
- B01J20/02—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
- B01J20/10—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising silica or silicate
- B01J20/16—Alumino-silicates
- B01J20/18—Synthetic zeolitic molecular sieves
- B01J20/183—Physical conditioning without chemical treatment, e.g. drying, granulating, coating, irradiation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
- B01J20/30—Processes for preparing, regenerating, or reactivating
- B01J20/3071—Washing or leaching
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
- B01J20/30—Processes for preparing, regenerating, or reactivating
- B01J20/3078—Thermal treatment, e.g. calcining or pyrolizing
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/10—Inorganic adsorbents
- B01D2253/106—Silica or silicates
- B01D2253/108—Zeolites
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/504—Carbon dioxide
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2220/00—Aspects relating to sorbent materials
- B01J2220/40—Aspects relating to the composition of sorbent or filter aid materials
- B01J2220/48—Sorbents characterised by the starting material used for their preparation
- B01J2220/4875—Sorbents characterised by the starting material used for their preparation the starting material being a waste, residue or of undefined composition
- B01J2220/4887—Residues, wastes, e.g. garbage, municipal or industrial sludges, compost, animal manure; fly-ashes
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
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- Chemical & Material Sciences (AREA)
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- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
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- Treating Waste Gases (AREA)
Abstract
The invention discloses a system and a method for manufacturing zeolite by using fly ash and capturing carbon dioxide in flue gas, relating to the field of flue gas treatment; the fly ash zeolite manufacturing system comprises a conveying device, a washing device, an acid washing device, a hydrothermal reaction device and a drying device; the conveying device comprises a rail weighbridge and a grab bucket, the grab bucket is connected to the rail weighbridge and can move along the rail weighbridge, and the flushing device, the pickling device, the hydrothermal reaction device and the drying device are all located on a moving route of the grab bucket; the fly ash zeolite carbon dioxide capturing system comprises a cooling device, a first connecting pipeline, a dewatering device, a second connecting pipeline, an adsorption device and a flue gas discharge pipeline, wherein the adsorbent of the adsorption device adopts fly ash zeolite. The invention has the advantages that: the fly ash can be utilized to produce zeolite and the fly ash zeolite can be utilized to capture carbon dioxide in flue gas.
Description
Technical Field
The invention relates to the field of flue gas treatment, in particular to a system and a method for manufacturing zeolite by using fly ash and capturing carbon dioxide in flue gas.
Background
The large consumption of coal generates a large amount of fly ash, and according to statistics, about 5 million tons of fly ash are generated in China every year, while the main treatment mode of the fly ash at present is simple storage or backfill, and the utilization rate is still very low.
Today, CO2The capture, sequestration and utilization technology (CCUS) is considered to be one of the most effective carbon emission reduction methods and is also an important means for carbon emission reduction of thermal power enterprises. The fly ash contains adsorbable CO2The magnetic beads and the like, SiO contained in fly ash2And Al2O3Is a suitable raw material for synthesizing zeolite, and the fly ash is prepared into the material capable of trapping CO2The fly ash zeolite can relieve the influence of the fly ash on the environment and can also realize carbon emission reduction. According to the literature, the fly ash zeolite adsorbs CO2The value can reach 190mg/g, which is much higher than the adsorption capacity 57.02mg/g of the magnetic beads of the fly ash in the separated fly ash.
Chinese patent CN201510116682.7 discloses a fluidized bed process for directly capturing carbon dioxide in mineralized flue gas, which utilizes high-calcium wastes such as fly ash, carbide slag, steel slag, waste cement and the like as raw materials, a bypass is opened on a flue gas discharge flue to lead a flue gas to be subjected to temperature and humidity adjustment through a temperature and humidity adjuster, the flue gas after temperature and humidity adjustment and the high-calcium wastes are subjected to contact reaction in a fluidized bed reactor to generate calcium carbonate, dust-containing gas discharged out of the fluidized bed reactor after reaction is sent to a cyclone separator for gas-solid separation, the obtained gas is sent back to an original flue gas discharge flue to be discharged into the flue gas, and a fluidized bed system for directly capturing carbon dioxide in mineralized flue gas is provided.
Chinese patent CN201520151601.2 discloses a fluidized bed system for directly capturing carbon dioxide in mineralized flue gas, comprising: the pretreatment unit comprises a dry powder grinder for grinding and/or a heating incinerator for heating treatment and/or a stirring reaction kettle for alkali desiliconization, a filter press and a drum dryer; the flue gas temperature and humidity adjusting unit is arranged on a bypass of the flue and comprises a bubble tower filled with liquid, and flue gas out of the bypass enters the bubble tower to realize temperature and humidity adjustment; the fluidized bed reactor is used for receiving the solid material of the pretreatment unit and the flue gas of the flue gas temperature and humidity adjusting unit; and the cyclone separator is connected with the dust-containing gas of the fluidized bed reactor to realize gas-solid separation, wherein the obtained gas is sent to a flue and discharged from a chimney.
Chinese patent CN201510217795.6 discloses a system device and a process for liquid phase indirect capture of carbon dioxide in mineralized flue gas, wherein the system device is arranged on a bypass of a flue and comprises an alkaline pretreatment unit, a fly ash CO capture unit, a fly ash carbonation unit and a separation and circulation unit, the main process of the process comprises five steps of desilication pretreatment, cyclic capture of CO in flue gas by clear liquid of a hydrocyclone in an absorption tower, carbonation in a clear liquid reaction kettle, carbonation in a slurry reaction kettle and reagent regeneration.
The technical scheme has the defects that the fly ash is not prepared into fly ash zeolite, the technologies of calcification, liquefaction and the like are adopted, and the technology is complicated; other pairs of fly ash zeolite, CO2Separation and other single and sporadic research technologies, no actual process system from production, and no direct use of fly ash zeolite for capturing CO in flue gas2The system of (1).
Disclosure of Invention
The invention aims to provide a system and a method for manufacturing zeolite and capturing carbon dioxide in flue gas by using fly ash, which can produce zeolite by using fly ash and capture carbon dioxide in flue gas by using fly ash zeolite.
The invention solves the technical problems through the following technical means: the system for manufacturing zeolite and capturing carbon dioxide in flue gas by utilizing fly ash comprises a fly ash zeolite manufacturing system (1) and a fly ash zeolite capturing carbon dioxide system (2);
the fly ash zeolite manufacturing system (1) comprises a conveying device (11), a washing device (12), an acid washing device (14), a hydrothermal reaction device (15) and a drying device (16); the conveying device (11) comprises a rail weighbridge (111) and a grab bucket (112), the grab bucket (112) is connected to the rail weighbridge (111) and can move along the rail weighbridge (111), and the flushing device (12), the pickling device (14), the hydrothermal reaction device (15) and the drying device (16) are all located on the moving route of the grab bucket (112);
fly ash zeolite entrapment carbon dioxide system (2) includes cooling device (22), first connecting tube (23), dewatering device (24), second connecting tube (25), adsorption equipment (26), flue gas emission pipeline (27), cooling device (22) passes through first connecting tube (23) are connected dewatering device (24), dewatering device (24) pass through second connecting tube (25) are connected adsorption equipment (26), adsorption equipment (26) pass through flue gas emission pipeline (27) connect the chimney, the adsorbent of adsorption equipment (26) adopts fly ash zeolite.
The main components of the fly ash, namely alumina and silicon dioxide, are utilized to prepare the fly ash zeolite, the method is simple, and the energy consumption is low; the utilization rate of the fly ash is improved, and the solid waste discharge of enterprises is reduced; the adsorption capacity of the fly ash zeolite is utilized to capture carbon dioxide in the flue gas, and simultaneously, the emission of sulfur dioxide and nitrogen oxide in the flue gas is reduced, and the pressure of desulfurization and denitrification is reduced; the fly ash zeolite after trapping the carbon dioxide can be neutralized, stored in carbon and used in carbon, and can be recycled for multiple times after releasing the carbon dioxide.
As an optimized technical scheme, the flushing device (12) comprises a first platform (121), a first return pipeline (122), a second platform (123), a second return pipeline (124) and a clean water pipeline (125), wherein the first platform (121) is connected with the pickling device (14) through the first return pipeline (122), the second platform (123) is connected with the hydrothermal reaction device (15) through the second return pipeline (124), and the clean water pipeline (125) stretches across the first platform (121) and the second platform (123). The first platform and the second platform can be used for respectively placing the pulverized fuel ash subjected to acid washing and the pulverized fuel ash zeolite subjected to hydrothermal reaction, discharging clear water through a clear water pipeline for washing, and can also be used for respectively airing the pulverized fuel ash and the pulverized fuel ash zeolite subjected to washing; the washing liquid on the first platform and the second platform can respectively flow back to the acid washing device and the hydrothermal reaction device through the first return pipeline and the second return pipeline, so that resources are saved.
As an optimized technical scheme, the fly ash zeolite manufacturing system (1) further comprises a fine ash separation device (13), the fine ash separation device (13) is connected with the acid washing device (14), the fine ash separation device (13) comprises a spiral separator (131), a fly ash conveying pipeline (132) and a fan (133), a fine ash outlet of the spiral separator (131) is connected with the acid washing device (14) through the fly ash conveying pipeline (132), and the fan (133) is installed on the fly ash conveying pipeline (132). The spiral separator can separate fine ash in the fly ash, the fine fly ash separated by the spiral separator can be conveyed to the acid cleaning device through the fly ash conveying pipeline by using the fan, the fine ash contains less impurities such as carbon and the like, the subsequent operation cost can be reduced, and the yield of the synthetic fly ash zeolite is improved;
as an optimized technical scheme, the pickling device (14) comprises a pickling tank (141), an acid adding pipeline (142) and a waste liquid pipeline (143), wherein the acid adding pipeline (142) and the waste liquid pipeline (143) are respectively positioned on two sides of the pickling tank (141) and are respectively communicated with the pickling tank (141). Hydrochloric acid is filled in the pickling tank, the concentration of the hydrochloric acid is reduced along with the increase of the pickling times, the hydrochloric acid can be added through the acid adding pipeline to maintain the concentration of the hydrochloric acid in the pickling tank, and waste liquid after pickling is discharged through the waste liquid pipeline.
As an optimized technical scheme, the hydrothermal reaction device (15) comprises a hydrothermal reaction kettle (151), an alkali adding pipeline (152) and a liquid discharging pipeline (153); the alkali adding pipeline (152) and the liquid discharging pipeline (153) are respectively positioned at two sides of the hydrothermal reaction kettle (151) and are respectively communicated with the hydrothermal reaction cavity; a hydrothermal reaction cavity and a first steam cavity are arranged in the hydrothermal reaction kettle (151), and the first steam cavity surrounds the outside of the hydrothermal reaction cavity and is independent from the hydrothermal reaction cavity; the hydrothermal reaction device (15) further comprises a first steam inlet pipeline (154), a first steam outlet pipeline (155) and a first water drainage pipeline (156); the first steam inlet pipeline (154) and the first steam outlet pipeline (155) are respectively positioned at two sides of the hydrothermal reaction kettle (151) and are respectively communicated with the first steam cavity; the first water drainage pipeline (156) is positioned below the hydrothermal reaction kettle (151) and communicated with the first steam cavity, and a first water drainage valve is arranged on the first water drainage pipeline (156);
the drying device (16) comprises a drying box (161), a second steam inlet pipeline (162), a second steam outlet pipeline (163) and a second drain pipeline (164); a drying cavity and a second steam cavity are arranged inside the drying box (161), and the second steam cavity surrounds the outside of the drying cavity and is independent from the drying cavity; the second steam inlet pipeline (162) and the second steam outlet pipeline (163) are respectively positioned at two sides of the drying box (161) and are respectively communicated with the second steam cavity, and the second steam outlet pipeline (163) is communicated with the first steam inlet pipeline (154); the second drain pipe (164) is located below the drying box (161) and communicated with the second steam cavity, and a second drain valve is arranged on the second drain pipe (164).
Sodium hydroxide solution can be added into the hydrothermal reaction cavity through an alkali adding pipeline, the fly ash and the added additive are subjected to hydrothermal reaction with the sodium hydroxide in the hydrothermal reaction cavity, and waste liquid of the hydrothermal reaction is discharged through a liquid discharging pipeline; the waste heat steam of electric power enterprise is more, adopts steam heating can recycle waste heat steam, resources are saved.
As an optimized technical scheme, the fly ash zeolite manufacturing system (1) further comprises a conveyor belt (17) and a crusher (18); the drying device (16) further comprises a gate (165), the gate (165) opening towards the conveyor belt (17), the drying device (16) being connected to the crusher (18) by means of the conveyor belt (17). The produced fly ash zeolite can be crushed by a crusher.
As an optimized technical scheme, the fly ash zeolite manufacturing system (1) further comprises a packer (19), wherein the packer (19) is connected to the outlet end of the crusher (18). One part of the crushed fly ash zeolite is directly conveyed to a fly ash zeolite carbon dioxide capturing system, and the rest of the crushed fly ash zeolite can be packed by a packing machine and then stored in a warehouse.
As an optimized technical scheme, the dehydration device (24) comprises a dehydration tower (241), a first flue gas inlet (242), a first flue gas outlet (243), a dehydrating agent feeding port (244), a dehydrating agent discharging port (245) and a material supporting plate (246); a dehydration cavity is arranged in the dehydration tower (241); the first flue gas inlet (242) is arranged at the lower part of the dehydration tower (241), and the first flue gas outlet (243) is arranged at the upper part of the dehydration tower (241); the dehydrating agent feeding port (244) is arranged at the upper part of the dehydrating tower (241), and the dehydrating agent discharging port (245) is arranged at the lower part of the dehydrating tower (241); the first flue gas inlet (242), the first flue gas outlet (243), the dehydrating agent feeding hole (244) and the dehydrating agent discharging hole (245) are respectively communicated with the dehydrating cavity; a plurality of stripper plates (246) are mounted in the dewatering cavity at an angle. The structure of the dehydration tower is beneficial to feeding and discharging, the contact area of the flue gas and the dehydrating agent is increased, and the dehydrating agent is beneficial to absorbing moisture in the flue gas.
As an optimized technical scheme, anhydrous calcium chloride is adopted as the dehydrating agent of the dehydrating device (24). The anhydrous calcium chloride has better dehydration performance than fly ash zeolite and can play a good role in drying flue gas; and does not absorb carbon dioxide, sulfur dioxide and the like, and can be repeatedly used.
As an optimized technical scheme, the adsorption device (26) comprises an adsorption tower (261), a second flue gas inlet (262), a second flue gas outlet (263), an adsorbent feeding hole (264) and an adsorbent discharging hole (265); an adsorption cavity is arranged inside the adsorption tower (261); the second flue gas inlet (262) is arranged at the lower part of the adsorption tower (261), and the second flue gas outlet (263) is arranged at the upper part of the adsorption tower (261); the adsorbent feeding port (264) is arranged at the upper part of the adsorption tower (261), and the adsorbent discharging port (265) is arranged at the lower part of the adsorption tower (261); and the second flue gas inlet (262), the second flue gas outlet (263), the adsorbent feeding hole (264) and the adsorbent discharging hole (265) are respectively communicated with the adsorption cavity.
As an optimized technical scheme, the fly ash zeolite carbon dioxide capturing system (2) further comprises a flue gas separation device (21), wherein the flue gas separation device (21) comprises a flue gas separation pipeline (211) and a fan (212); the flue gas separation pipeline (211) is divided into two paths, wherein one path is connected with the cooling device (22), and the other path is connected with a chimney; the fan (212) is arranged on the way that the flue gas separation pipeline (211) is connected with the cooling device (22). The method is suitable for the flue gas only needing to remove carbon dioxide, one part of the flue gas enters a cooling device, the rest of the flue gas enters a chimney to be discharged, and when the amount of the fly ash zeolite is not enough, the method is suitable for continuous production by separating one part of the flue gas.
As the optimized technical scheme, the fly ash zeolite carbon dioxide capturing system (2) further comprises a flue gas separation device (21), the flue gas separation device (21) comprises a flue gas separation pipeline (211), a fan (212) and a desulfurizing tower (213), the flue gas separation pipeline (211) is divided into two paths, one path is connected with the cooling device (22), the other path is connected with the desulfurizing tower (213), and the desulfurizing tower (213) is connected with a chimney. The device is suitable for removing carbon dioxide and simultaneously removing sulfur and nitrogen in flue gas, wherein a part of the flue gas enters a cooling device, and the rest of the flue gas enters a desulfurizing tower for desulfurization and then enters a chimney for emission.
As an optimized technical scheme, the number of the adsorption devices (26) is two, the two adsorption devices (26) are connected in series, and the two adsorption devices (26) are a first-stage adsorption device and a second-stage adsorption device in sequence. The fly ash zeolite in the first-stage absorption device absorbs sulfur dioxide and nitrogen oxides in the flue gas, the fly ash zeolite in the second-stage absorption device absorbs carbon dioxide in the flue gas, and the fly ash zeolite after absorbing carbon dioxide and nitrogen oxides can be used for preparing acid in a sulfuric acid plant.
As an optimized technical scheme, the cooling device (22) adopts a low-temperature economizer.
As an optimized technical scheme, a plurality of cooling devices (22) are arranged, and the cooling devices (22) are connected in series. Is suitable for flue gas with large water content, and reduces the water content before the flue gas enters the dehydration device through a plurality of cooling devices
The method for manufacturing zeolite and capturing carbon dioxide in flue gas by utilizing fly ash comprises the following steps:
separating fine ash from the fly ash through gravity settling, and conveying the separated fine ash to an acid cleaning device (14);
secondly, hydrochloric acid is filled in the acid cleaning device (14), the fly ash is soaked in the acid cleaning device (14), and impurities in the fly ash are washed away;
moving the grab bucket (112) to the upper part in the acid cleaning device (14) along the track scale (111), stretching into the acid cleaning device (14) to grab the fly ash and conveying the fly ash to the flushing device (12), flushing the washed fly ash by the flushing device (12), and airing the flushed fly ash on the flushing device (12);
fourthly, the grab bucket (112) grabs the coal ash from the washing device (12), moves the coal ash to the upper part of the hydrothermal reaction device (15) along the track scale (111), and puts the coal ash into the hydrothermal reaction device (15); simultaneously, adding additives containing silicon and aluminum into the hydrothermal reaction device (15); then adding a sodium hydroxide solution, the fly ash and the added additive to perform hydrothermal reaction with sodium hydroxide in a hydrothermal reaction cavity to prepare fly ash zeolite;
fifthly, the grab bucket (112) extends into the hydrothermal reaction device (15) to grab the reacted fly ash zeolite and convey the fly ash zeolite to the washing device (12), the washing device (12) washes the fly ash zeolite, and the washed fly ash zeolite is dried on the washing device (12);
sixthly, the grab bucket (112) grabs the fly ash zeolite from the washing device (12), moves the fly ash zeolite to the upper part of the drying device (16) along the track scale (111), and puts the fly ash zeolite into the drying device (16) for drying;
step seven, crushing the dried fly ash zeolite, conveying a part of the crushed fly ash zeolite into an adsorption device (26), sealing and packaging the rest, and storing in a warehouse;
step eight, separating the flue gas, enabling a part of the flue gas to enter a cooling device (22), and enabling the rest of the flue gas to enter a chimney for emission;
step nine, the cooling device (22) cools and dehydrates the flue gas, and then the flue gas enters the dehydration device (24) from the first connecting pipeline (23) for dehydration;
step ten, the dehydrated flue gas enters an adsorption device (26) through a second connecting pipeline (25), the fly ash zeolite adsorbs carbon dioxide in the flue gas, and then the flue gas enters a chimney through a flue gas discharge pipeline (27) to be discharged.
The invention has the advantages that: the main components of the fly ash, namely alumina and silicon dioxide, are utilized to prepare the fly ash zeolite, the method is simple, and the energy consumption is low; the utilization rate of the fly ash is improved, and the solid waste discharge of enterprises is reduced; at present, a system for capturing carbon dioxide by using fly ash zeolite is not used, the prior art is that the carbon dioxide is directly stored or neutralized after being separated, the adsorption capacity of the fly ash zeolite is utilized to capture the carbon dioxide in the flue gas, the emission of sulfur dioxide and nitrogen oxide in the flue gas is reduced, and the pressure of desulfurization and denitrification is reduced; the fly ash zeolite after trapping the carbon dioxide can be neutralized, stored in carbon and used in carbon, and can be recycled for multiple times after releasing the carbon dioxide.
Drawings
FIG. 1 is a schematic diagram of a system for producing zeolite and capturing carbon dioxide in flue gas by using fly ash according to an embodiment of the present invention.
FIG. 2 is a schematic diagram of the fine ash separator, the pickling unit, a part of the conveyor, and the washing unit according to the embodiment of the present invention.
FIG. 3 is a schematic view showing the structure of a hydrothermal reaction apparatus, a part of a transport apparatus, and a washing apparatus according to an embodiment of the present invention.
Fig. 4 is a schematic structural diagram of a drying apparatus according to an embodiment of the present invention.
FIG. 5 is a schematic structural diagram of a dewatering device according to an embodiment of the present invention.
FIG. 6 is a schematic view of an embodiment of an absorbent device of the present invention.
FIG. 7 is a schematic diagram of a system for capturing carbon dioxide using a fly ash zeolite according to example two of the present invention.
FIG. 8 is a schematic diagram of a carbon dioxide capture system using a fly ash zeolite according to an embodiment of the present invention.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the embodiments of the present invention, and it is obvious that the described embodiments are some embodiments of the present invention, but not all embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Example one
A system for manufacturing zeolite by utilizing fly ash and capturing carbon dioxide in flue gas comprises a zeolite manufacturing system 1 and a fly ash zeolite capturing carbon dioxide system 2.
As shown in fig. 1, the fly ash zeolite production system 1 includes a conveyor 11, a washing device 12, a fine ash separation device 13, a pickling device 14, a hydrothermal reaction device 15, a drying device 16, a conveyor 17, a crusher 18, and a baler 19.
The conveying device 11 comprises a rail weighbridge 111 and a grab bucket 112, wherein the grab bucket 112 is connected to the rail weighbridge 111 and can move along the rail weighbridge 111; the fine ash separation device 13, the acid washing device 14, the hydrothermal reaction device 15 and the drying device 16 are all positioned below the rail weighbridge 111 and are sequentially arranged in a row along the length direction of the rail weighbridge 111, and the flushing device 12 is positioned below the rail weighbridge 111 and is positioned above the fine ash separation device 13, the acid washing device 14, the hydrothermal reaction device 15 and the drying device 16; the washing device 12, the pickling device 14, the hydrothermal reaction device 15 and the drying device 16 are all located on a moving route of the grab bucket 112, the fine ash separation device 13 is connected with the pickling device 14, the drying device 16 is connected with the crusher 18 through a conveyor belt 17, and the packing machine 19 is connected with the outlet end of the crusher 18.
The washing device 12 comprises a first platform 121, a first return pipeline 122, a second platform 123, a second return pipeline 124 and a clean water pipeline 125, wherein the first platform 121 is positioned above the pickling device 14, the first platform 121 is connected with the pickling device 14 through the first return pipeline 122, the second platform is positioned above the hydrothermal reaction device 15, the second platform 123 is connected with the hydrothermal reaction device 15 through the second return pipeline 124, and the clean water pipeline 125 spans above the first platform 121 and the second platform 123.
As shown in fig. 2, the fine ash separation device 13 includes a spiral separator 131, a fly ash conveying pipe 132, a first fan 133; the spiral separator 131 is arranged in the fly ash workshop, the spiral separator 131 is provided with a sampling port, a fine ash outlet of the spiral separator 131 is connected with the pickling device 14 through a fly ash conveying pipeline 132, and the first fan 133 is arranged on the fly ash conveying pipeline 132.
The pickling device 14 comprises a pickling tank 141, an acid adding pipeline 142 and a waste liquid pipeline 143, wherein the acid adding pipeline 142 and the waste liquid pipeline 143 are respectively positioned at two sides of the pickling tank 141 and are respectively communicated with the pickling tank 141, and valves are respectively arranged on the acid adding pipeline 142 and the waste liquid pipeline 143.
As shown in fig. 3, the hydrothermal reaction device 15 includes a hydrothermal reaction kettle 151, an alkali adding pipeline 152, a liquid discharging pipeline 153, a first steam inlet pipeline 154, a first steam outlet pipeline 155, and a first water drainage pipeline 156; a hydrothermal reaction cavity and a first steam cavity are arranged in the hydrothermal reaction kettle 151, and the first steam cavity surrounds the outside of the hydrothermal reaction cavity and is independent from the hydrothermal reaction cavity; the alkali adding pipeline 152 and the liquid discharging pipeline 153 are respectively positioned at two sides of the hydrothermal reaction kettle 151 and are respectively communicated with the hydrothermal reaction cavity, and valves are respectively arranged on the alkali adding pipeline 152 and the liquid discharging pipeline 153; the second return pipe 124 is communicated with the hydrothermal reaction cavity; the first steam inlet pipeline 154 and the first steam outlet pipeline 155 are respectively located at two sides of the hydrothermal reaction kettle 151 and are respectively communicated with the first steam cavity, and valves are respectively arranged on the first steam inlet pipeline 154 and the first steam outlet pipeline 155; the first drain pipe 156 is located below the hydrothermal reaction kettle 151 and communicated with the first steam cavity, and a first drain valve is arranged on the first drain pipe 156.
As shown in fig. 4, the drying device 16 includes a drying box 161, a second steam inlet pipe 162, a second steam outlet pipe 163, a second drain pipe 164, and a shutter 165; a drying cavity and a second steam cavity are arranged inside the drying box 161, and the second steam cavity surrounds the outside of the drying cavity and is independent from the drying cavity; the second steam inlet pipeline 162 and the second steam outlet pipeline 163 are respectively positioned at two sides of the drying box 161 and are respectively communicated with the second steam cavity, a valve is arranged on the second steam inlet pipeline 162, and the second steam outlet pipeline 163 is communicated with the first steam inlet pipeline 154; the second drain pipe 164 is located below the drying box 161 and communicated with the second steam cavity, and a second drain valve is arranged on the second drain pipe 164; a shutter 165 is installed at one side of the drying cabinet 161, and the opening of the shutter 165 is directed toward the entrance end of the conveyor 17.
As shown in fig. 1, the fly ash zeolite carbon dioxide capturing system 2 comprises a flue gas separation device 21, a cooling device 22, a first connecting pipeline 23, a dehydration device 24, a second connecting pipeline 25, an adsorption device 26 and a flue gas discharge pipeline 27.
The flue gas separation device 21 comprises a flue gas separation pipeline 211 and a second fan 212; the flue gas separation pipe 211 is divided into two paths, wherein one path is connected with the cooling device 22, and the other path is connected with a chimney; the second fan 212 is installed on one path of the flue gas separation pipeline 211 connected with the cooling device 22; the cooling device 22 adopts a low-temperature economizer, the cooling device 22 is connected with a dehydrating device 24 through a first connecting pipeline 23, the dehydrating device 24 is connected with an adsorbing device 26 through a second connecting pipeline 25, and the adsorbing device 26 is connected with a chimney through a flue gas discharge pipeline 27.
As shown in fig. 5, the dehydration device 24 includes a dehydration tower 241, a first flue gas inlet 242, a first flue gas outlet 243, a dehydrating agent feed inlet 244, a dehydrating agent discharge outlet 245, and a retainer plate 246; a dehydration cavity is arranged in the dehydration tower 241; the first flue gas inlet 242 is arranged at the lower part of the dehydrating tower 241, and the first flue gas outlet 243 is arranged at the upper part of the dehydrating tower 241; a dehydrating agent feed port 244 is arranged at the upper part of the dehydrating tower 241, and a dehydrating agent discharge port 245 is arranged at the lower part of the dehydrating tower 241; the first flue gas inlet 242, the first flue gas outlet 243, the dehydrating agent feeding hole 244 and the dehydrating agent discharging hole 245 are respectively communicated with the dehydrating cavity; a plurality of stripper plates 246 are installed in the dehydration cavity in an inclined manner; the dehydrating agent of the dehydrating device 24 adopts anhydrous calcium chloride, the dehydrating performance of the anhydrous calcium chloride is better than that of fly ash zeolite, and the dehydrating agent can play a good role in drying flue gas; and does not absorb carbon dioxide, sulfur dioxide and the like, and can be repeatedly used.
As shown in fig. 6, the adsorption device 26 includes an adsorption tower 261, a second flue gas inlet 262, a second flue gas outlet 263, an adsorbent feeding port 264, and an adsorbent discharging port 265; an adsorption cavity is arranged inside the adsorption tower 261; the second flue gas inlet 262 is arranged at the lower part of the adsorption tower 261, and the second flue gas outlet 263 is arranged at the upper part of the adsorption tower 261; the adsorbent feed inlet 264 is arranged at the upper part of the adsorption tower 261, and the adsorbent discharge outlet 265 is arranged at the lower part of the adsorption tower 261; the second flue gas inlet 262, the second flue gas outlet 263, the adsorbent feeding hole 264 and the adsorbent discharging hole 265 are respectively communicated with the adsorption cavity; the adsorbent of the adsorption device 26 is fly ash zeolite.
The system for manufacturing zeolite and capturing carbon dioxide in flue gas by utilizing fly ash is suitable for flue gas which only needs to remove carbon dioxide and does not need to remove sulfur and nitrogen.
The method for manufacturing zeolite and capturing carbon dioxide in flue gas by utilizing fly ash comprises the following steps:
firstly, separating fine ash from the fly ash by a spiral separator 131 through gravity settling, wherein the number of the separated fine ash is less than 200 meshes; a fine ash sample is extracted from the sampling port for detection, and preparation is made for later additive adjustment; the fine fly ash separated by the spiral separator 131 is conveyed to the acid washing device 14 through the fly ash conveying pipe 132 by the first fan 133.
Soaking the fly ash in a pickling tank 141 for 2 hours, and washing off impurities in the fly ash; the pickling tank 141 is filled with 4.5% -5.5% hydrochloric acid, the concentration of the hydrochloric acid is reduced along with the increase of the pickling times, and the hydrochloric acid concentration in the pickling tank 141 is maintained by adding acid successively through an acid adding pipeline 142 connected with an acid storage tank; the waste liquid after pickling is discharged through the waste liquid pipe 143.
Moving the grab bucket 112 to the upper part of the pickling tank 141 along the rail weighbridge 111, stretching into the pickling tank 141 to grab the fly ash and conveying the fly ash to the first platform 121; the clean water pipeline 125 discharges clean water to wash the washed fly ash until the washing liquid is neutral, and the washed fly ash is dried on the first platform 121; the washing liquid on the first stage 121 is returned to the pickling tank 141 through the first return pipe 122.
Fourthly, the grab bucket 112 grabs the coal ash from the first platform 121, moves to the position above the hydrothermal reaction kettle 151 along the rail balance 111, opens a door above the hydrothermal reaction kettle 151, and puts the coal ash into the hydrothermal reaction cavity; simultaneously, adding an additive containing silicon and aluminum into the hydrothermal reaction cavity, wherein the components of the additive are determined according to the components of the fine ash sample detected in the step one, and the adjustment of the additive influences the floating of the yield of the fly ash zeolite; then closing the upper door of the hydrothermal reaction kettle 151, adding 2-3 mol/L sodium hydroxide solution through an alkali adding pipeline 152, carrying out hydrothermal reaction on the fly ash and the added additive and the sodium hydroxide in a hydrothermal reaction cavity for 18 hours, preparing fly ash zeolite by using main components of the fly ash, namely alumina and silica, and discharging waste liquid of the hydrothermal reaction through a liquid discharging pipeline 153; steam enters the first steam cavity through the first steam inlet pipe 154 and is discharged through the first steam outlet pipe 155, the hydrothermal reaction cavity is heated, the heating temperature is about 90 ℃, and condensed water in the first steam cavity is discharged through the first drain pipe 156.
Step five, the grab bucket 112 extends into the hydrothermal reaction cavity to grab the fly ash zeolite generated by the reaction to the second platform 123, the clean water pipeline 125 discharges clean water to wash the fly ash zeolite until the washing liquid is neutral, the washed fly ash zeolite is dried on the second platform 123, and the washing liquid on the second platform 123 flows back to the hydrothermal reaction cavity through the second backflow pipeline 124.
Step six, the grab bucket 112 grabs the fly ash zeolite from the second platform 123, moves to the upper part of the drying box 161 along the track balance 111, opens the box cover above the drying box 161, and puts the fly ash zeolite into the drying cavity for drying for 8 hours; steam enters the second steam cavity through the second steam inlet pipe 162 and is discharged through the second steam outlet pipe 163 to heat the drying cavity, and condensed water in the second steam cavity is discharged through the second drain pipe 164; the waste heat steam of the power enterprise is more, and the waste heat steam can be recycled by adopting steam heating, so that resources are saved.
Step seven, opening the gate 165, conveying the dried fly ash zeolite to a crusher 18 through a conveyor belt 17 for crushing, conveying a part of the crushed fly ash zeolite to an adsorption cavity through an adsorbent feeding hole 264, and hermetically packaging the rest of the crushed fly ash zeolite by a snakeskin bag with an inner container through a packaging machine 19 for storage.
Step eight, separating the flue gas by the flue gas separation device 21, and enabling a part of the flue gas to enter the cooling device 22 from one path of the flue gas separation pipeline 211 by using the second fan 212, and enabling the rest of the flue gas to enter a chimney for emission from the other path of the flue gas separation pipeline 211; because the flue gas volume of the flue gas pipeline is large, when the fly ash zeolite volume is insufficient, a part of flue gas is separated, so that the continuous production is more suitable, and when the fly ash zeolite volume is sufficient, all the flue gas can enter subsequent equipment.
Step nine, the cooling device 22 cools and dehydrates the flue gas, and then the flue gas enters the dehydration device 24 from the first connecting pipeline 23 to be dehydrated.
Step ten, the dehydrated flue gas enters an adsorption device 26 through a second connecting pipeline 25, the fly ash zeolite adsorbs carbon dioxide in the flue gas, and then the flue gas enters a chimney through a flue gas discharge pipeline 27 to be discharged; the fly ash zeolite after trapping the carbon dioxide can be neutralized, stored in carbon and used in carbon, and can be recycled for multiple times after releasing the carbon dioxide.
Example two
As shown in fig. 7, the system for producing zeolite and capturing carbon dioxide in flue gas by using fly ash in this embodiment is different from the system in the first embodiment in that: two cooling devices 22 are provided, and the two cooling devices 22 are connected in series.
The system for manufacturing zeolite and capturing carbon dioxide in flue gas by utilizing fly ash in the embodiment is suitable for flue gas with large water content and without sulfur and nitrogen removal, and reduces the water content of the flue gas before the flue gas enters the dehydration device 24 through the two cooling devices 22 connected in series.
EXAMPLE III
As shown in fig. 8, the system for producing zeolite and capturing carbon dioxide in flue gas by using fly ash in this embodiment is different from the system in the first embodiment in that: the flue gas separation device 21 comprises a flue gas separation pipeline 211, a fan 212 and a desulfurizing tower 213; the flue gas separation pipeline 211 is divided into two paths, the other path is connected with the cooling device 22, the other path is connected with the desulfurizing tower 213, and the desulfurizing tower 213 is connected with a chimney; adsorption equipment 26 is equipped with two, two adsorption equipment 26 series connection, and two adsorption equipment 26 are one-level adsorption equipment and second grade adsorption equipment in proper order.
The system for manufacturing zeolite and capturing carbon dioxide in flue gas by utilizing fly ash is suitable for removing carbon dioxide and simultaneously removing sulfur and nitrogen in flue gas.
The method for manufacturing zeolite by using fly ash and capturing carbon dioxide in flue gas in the embodiment is different from the first embodiment in that:
step eight, separating the flue gas by the flue gas separation device 21, enabling a part of the flue gas to enter the cooling device 22 from one path of the flue gas separation pipeline 211 by using the fan 212, enabling the rest of the flue gas to enter the desulfurizing tower 213 from the other path of the flue gas separation pipeline 211, desulfurizing by the desulfurizing tower 213, and then discharging in a chimney; because the flue gas volume of the flue gas pipeline is large, when the fly ash zeolite volume is insufficient, a part of flue gas is separated, so that the continuous production is more suitable, and when the fly ash zeolite volume is sufficient, all the flue gas can enter subsequent equipment.
Step ten, the dehydrated flue gas sequentially enters a first-stage adsorption device and a second-stage adsorption device through a second connecting pipeline 25, the fly ash zeolite in the first-stage adsorption device adsorbs sulfur dioxide and nitrogen oxide in the flue gas, the fly ash zeolite in the second-stage adsorption device adsorbs carbon dioxide in the flue gas, and then the flue gas enters a chimney through a flue gas discharge pipeline 27 to be discharged; the content of the fly ash zeolite filler in the first-stage adsorption device is controlled according to the concentration of carbon dioxide and nitrogen oxide in the flue gas and the speed of the flue gas so as to ensure the whole adsorption and avoid the impurity of the carbon dioxide trapped by the fly ash zeolite in the second-stage adsorption device, the content of the carbon dioxide in the flue gas entering the second-stage adsorption device is 10-15 percent, and the content of the carbon trapped by the fly ash zeolite in the second-stage adsorption device is higher; the fly ash zeolite in the first-stage adsorption device after adsorbing carbon dioxide and nitrogen oxide can be directly sent to a sulfuric acid plant, and the concentration of sulfur dioxide is improved through heating desorption, so that the fly ash zeolite is used for preparing sulfuric acid in the sulfuric acid plant, and liquid sulfur dioxide or other sulfites can be prepared according to specific conditions.
The above examples are only intended to illustrate the technical solution of the present invention, but not to limit it; although the present invention has been described in detail with reference to the foregoing embodiments, it will be understood by those of ordinary skill in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some technical features may be equivalently replaced; and such modifications or substitutions do not depart from the spirit and scope of the corresponding technical solutions of the embodiments of the present invention.
Claims (10)
1. A system for manufacturing zeolite and capturing carbon dioxide in flue gas by utilizing fly ash is characterized in that: comprises a fly ash zeolite manufacturing system (1) and a fly ash zeolite carbon dioxide capturing system (2);
the fly ash zeolite manufacturing system (1) comprises a conveying device (11), a washing device (12), an acid washing device (14), a hydrothermal reaction device (15) and a drying device (16); the conveying device (11) comprises a rail weighbridge (111) and a grab bucket (112), the grab bucket (112) is connected to the rail weighbridge (111) and can move along the rail weighbridge (111), and the flushing device (12), the pickling device (14), the hydrothermal reaction device (15) and the drying device (16) are all located on the moving route of the grab bucket (112);
fly ash zeolite entrapment carbon dioxide system (2) includes cooling device (22), first connecting tube (23), dewatering device (24), second connecting tube (25), adsorption equipment (26), flue gas emission pipeline (27), cooling device (22) passes through first connecting tube (23) are connected dewatering device (24), dewatering device (24) pass through second connecting tube (25) are connected adsorption equipment (26), adsorption equipment (26) pass through flue gas emission pipeline (27) connect the chimney, the adsorbent of adsorption equipment (26) adopts fly ash zeolite.
2. The system for producing zeolite and capturing carbon dioxide in flue gas using fly ash as claimed in claim 1, wherein: the washing device (12) comprises a first platform (121), a first return pipeline (122), a second platform (123), a second return pipeline (124) and a clean water pipeline (125), wherein the first platform (121) is connected with the pickling device (14) through the first return pipeline (122), the second platform (123) is connected with the hydrothermal reaction device (15) through the second return pipeline (124), and the clean water pipeline (125) spans above the first platform (121) and the second platform (123).
3. The system for producing zeolite and capturing carbon dioxide in flue gas using fly ash as claimed in claim 1, wherein: the fly ash zeolite manufacturing system (1) further comprises a fine ash separation device (13), the fine ash separation device (13) is connected with the acid washing device (14), the fine ash separation device (13) comprises a spiral separator (131), a fly ash conveying pipeline (132) and a fan (133), a fine ash outlet of the spiral separator (131) is connected with the acid washing device (14) through the fly ash conveying pipeline (132), and the fan (133) is installed on the fly ash conveying pipeline (132).
4. The system for producing zeolite and capturing carbon dioxide in flue gas using fly ash as claimed in claim 1, wherein: the hydrothermal reaction device (15) comprises a hydrothermal reaction kettle (151), a hydrothermal reaction cavity and a first steam cavity are arranged inside the hydrothermal reaction kettle (151), and the first steam cavity surrounds the outside of the hydrothermal reaction cavity and is independent from the hydrothermal reaction cavity; the hydrothermal reaction device (15) further comprises a first steam inlet pipeline (154), a first steam outlet pipeline (155) and a first water drainage pipeline (156); the first steam inlet pipeline (154) and the first steam outlet pipeline (155) are respectively positioned at two sides of the hydrothermal reaction kettle (151) and are respectively communicated with the first steam cavity; the first water drainage pipeline (156) is positioned below the hydrothermal reaction kettle (151) and communicated with the first steam cavity, and a first water drainage valve is arranged on the first water drainage pipeline (156);
the drying device (16) comprises a drying box (161), a second steam inlet pipeline (162), a second steam outlet pipeline (163) and a second drain pipeline (164); a drying cavity and a second steam cavity are arranged inside the drying box (161), and the second steam cavity surrounds the outside of the drying cavity and is independent from the drying cavity; the second steam inlet pipeline (162) and the second steam outlet pipeline (163) are respectively positioned at two sides of the drying box (161) and are respectively communicated with the second steam cavity, and the second steam outlet pipeline (163) is communicated with the first steam inlet pipeline (154); the second drain pipe (164) is located below the drying box (161) and communicated with the second steam cavity, and a second drain valve is arranged on the second drain pipe (164).
5. The system for producing zeolite and capturing carbon dioxide in flue gas using fly ash as claimed in claim 1, wherein: the dehydration device (24) comprises a dehydration tower (241), a first flue gas inlet (242), a first flue gas outlet (243), a dehydrating agent feeding port (244), a dehydrating agent discharging port (245) and a material supporting plate (246); a dehydration cavity is arranged in the dehydration tower (241); the first flue gas inlet (242) is arranged at the lower part of the dehydration tower (241), and the first flue gas outlet (243) is arranged at the upper part of the dehydration tower (241); the dehydrating agent feeding port (244) is arranged at the upper part of the dehydrating tower (241), and the dehydrating agent discharging port (245) is arranged at the lower part of the dehydrating tower (241); the first flue gas inlet (242), the first flue gas outlet (243), the dehydrating agent feeding hole (244) and the dehydrating agent discharging hole (245) are respectively communicated with the dehydrating cavity; a plurality of stripper plates (246) are mounted in the dewatering cavity at an angle.
6. The system for producing zeolite and capturing carbon dioxide in flue gas using fly ash as claimed in claim 1, wherein: the fly ash zeolite carbon dioxide capturing system (2) further comprises a flue gas separation device (21), wherein the flue gas separation device (21) comprises a flue gas separation pipeline (211) and a fan (212); the flue gas separation pipeline (211) is divided into two paths, wherein one path is connected with the cooling device (22), and the other path is connected with a chimney; the fan (212) is arranged on the way that the flue gas separation pipeline (211) is connected with the cooling device (22).
7. The system for producing zeolite and capturing carbon dioxide in flue gas using fly ash as claimed in claim 1, wherein: fly ash zeolite entrapment carbon dioxide system (2) still includes gas separation device (21), gas separation device (21) include gas separation pipeline (211), fan (212), desulfurizing tower (213), gas separation pipeline (211) divide into two the tunnel, wherein connect all the way cooling device (22), another way is connected desulfurizing tower (213), chimney is connected in desulfurizing tower (213).
8. The system for producing zeolite and capturing carbon dioxide in flue gas using fly ash as claimed in claim 7, wherein: adsorption equipment (26) are equipped with two, two adsorption equipment (26) series connection, and two adsorption equipment (26) are one-level adsorption equipment and second grade adsorption equipment in proper order.
9. The system for producing zeolite and capturing carbon dioxide in flue gas using fly ash as claimed in claim 1, wherein: the cooling devices (22) are provided in plurality, and the cooling devices (22) are connected in series.
10. A method for manufacturing zeolite and capturing carbon dioxide in flue gas by using fly ash is characterized by comprising the following steps:
separating fine ash from the fly ash through gravity settling, and conveying the separated fine ash to an acid cleaning device (14);
secondly, hydrochloric acid is filled in the acid cleaning device (14), the fly ash is soaked in the acid cleaning device (14), and impurities in the fly ash are washed away;
moving the grab bucket (112) to the upper part in the acid cleaning device (14) along the track scale (111), stretching into the acid cleaning device (14) to grab the fly ash and conveying the fly ash to the flushing device (12), flushing the washed fly ash by the flushing device (12), and airing the flushed fly ash on the flushing device (12);
fourthly, the grab bucket (112) grabs the coal ash from the washing device (12), moves the coal ash to the upper part of the hydrothermal reaction device (15) along the track scale (111), and puts the coal ash into the hydrothermal reaction device (15); simultaneously, adding additives containing silicon and aluminum into the hydrothermal reaction device (15); then adding a sodium hydroxide solution, the fly ash and the added additive to perform hydrothermal reaction with sodium hydroxide in a hydrothermal reaction cavity to prepare fly ash zeolite;
fifthly, the grab bucket (112) extends into the hydrothermal reaction device (15) to grab the reacted fly ash zeolite and convey the fly ash zeolite to the washing device (12), the washing device (12) washes the fly ash zeolite, and the washed fly ash zeolite is dried on the washing device (12);
sixthly, the grab bucket (112) grabs the fly ash zeolite from the washing device (12), moves the fly ash zeolite to the upper part of the drying device (16) along the track scale (111), and puts the fly ash zeolite into the drying device (16) for drying;
step seven, crushing the dried fly ash zeolite, conveying a part of the crushed fly ash zeolite into an adsorption device (26), sealing and packaging the rest, and storing in a warehouse;
step eight, separating the flue gas, enabling a part of the flue gas to enter a cooling device (22), and enabling the rest of the flue gas to enter a chimney for emission;
step nine, cooling and dewatering the flue gas by a cooling device (22), and then enabling the flue gas to enter a dewatering device (24) from a first connecting pipeline (23) for dewatering;
step ten, the dehydrated flue gas enters an adsorption device (26) through a second connecting pipeline (25), the fly ash zeolite adsorbs carbon dioxide in the flue gas, and then the flue gas enters a chimney through a flue gas discharge pipeline (27) to be discharged.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2023226473A1 (en) * | 2022-05-23 | 2023-11-30 | 中国华能集团清洁能源技术研究院有限公司 | Cooperative utilization system for coal gangue power generation and co2 mineralization and working method |
Citations (19)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH07165418A (en) * | 1993-12-13 | 1995-06-27 | Minako Ishikawa | Production of zeolite |
| CN2299308Y (en) * | 1996-06-07 | 1998-12-02 | 罗放明 | Dynamic railroad track scale grab bucket scale |
| CN1289652A (en) * | 2000-10-30 | 2001-04-04 | 华电环保系统工程有限公司 | Quickly loaded separating system of powdered coal ash |
| JP2002338970A (en) * | 2001-05-17 | 2002-11-27 | Nikkiso Co Ltd | System for effectively treating waste |
| CN1389399A (en) * | 2002-07-08 | 2003-01-08 | 中国地质大学（武汉） | Synthesis of zeolite with flyash |
| KR20040107655A (en) * | 2003-06-09 | 2004-12-23 | 대한민국(관리부서:농촌진흥청) | Mass Production Method for Artificial Zeolite |
| JP2005060212A (en) * | 2003-08-19 | 2005-03-10 | Katsuhiro Ito | Method and apparatus for manufacturing synthetic zeolite using sodium hydroxide and fly ash |
| CN1759938A (en) * | 2005-09-29 | 2006-04-19 | 河北衡丰发电有限责任公司 | Method for feeding fly ash in electric power plant |
| CN101503202A (en) * | 2009-02-11 | 2009-08-12 | 陕西理工学院 | Technique for hydro-thermal synthesis of high purity zeolite and fly ash zeolite adsorbing agent from fly ash |
| CN105253639A (en) * | 2015-10-15 | 2016-01-20 | 浙江工业大学 | Hydraulically-driven moving type spiral coal ash conveying device and operation method thereof |
| CN205139076U (en) * | 2015-11-20 | 2016-04-06 | 西安工业大学 | Full automatization water quality safety detection device based on intelligent machine arm |
| CN106495181A (en) * | 2016-10-26 | 2017-03-15 | 天津大学 | A kind of method that flyash synthesizes y-type zeolite |
| CN106865565A (en) * | 2017-03-26 | 2017-06-20 | 天津大学 | A kind of flyash synthesizes the method for X-type zeolite |
| CN109055957A (en) * | 2018-08-28 | 2018-12-21 | 格林美（武汉）城市矿产循环产业园开发有限公司 | A kind of intelligence pickling system |
| CN111068612A (en) * | 2019-12-31 | 2020-04-28 | 中国建筑材料科学研究总院有限公司 | Method for preparing zeolite-like porous material by using solid waste, zeolite-like porous material and application thereof |
| CN112263890A (en) * | 2020-09-10 | 2021-01-26 | 国电新能源技术研究院有限公司 | Flue gas waste heat utilization type carbon capture method and system |
| CN113005466A (en) * | 2021-03-24 | 2021-06-22 | 广东邦普循环科技有限公司 | Safe pickling equipment and method |
| CN113144818A (en) * | 2021-04-29 | 2021-07-23 | 华电宁夏灵武发电有限公司 | Fly ash-based carbon dioxide absorption system and fly ash recycling method for absorbing carbon dioxide |
| CN113353949A (en) * | 2021-06-30 | 2021-09-07 | 东北大学 | Synthetic zeolite of fly ash and coal gangue aluminum extraction slag and comprehensive utilization method thereof |
-
2021
- 2021-09-08 CN CN202111049652.0A patent/CN113996142B/en active Active
Patent Citations (19)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH07165418A (en) * | 1993-12-13 | 1995-06-27 | Minako Ishikawa | Production of zeolite |
| CN2299308Y (en) * | 1996-06-07 | 1998-12-02 | 罗放明 | Dynamic railroad track scale grab bucket scale |
| CN1289652A (en) * | 2000-10-30 | 2001-04-04 | 华电环保系统工程有限公司 | Quickly loaded separating system of powdered coal ash |
| JP2002338970A (en) * | 2001-05-17 | 2002-11-27 | Nikkiso Co Ltd | System for effectively treating waste |
| CN1389399A (en) * | 2002-07-08 | 2003-01-08 | 中国地质大学（武汉） | Synthesis of zeolite with flyash |
| KR20040107655A (en) * | 2003-06-09 | 2004-12-23 | 대한민국(관리부서:농촌진흥청) | Mass Production Method for Artificial Zeolite |
| JP2005060212A (en) * | 2003-08-19 | 2005-03-10 | Katsuhiro Ito | Method and apparatus for manufacturing synthetic zeolite using sodium hydroxide and fly ash |
| CN1759938A (en) * | 2005-09-29 | 2006-04-19 | 河北衡丰发电有限责任公司 | Method for feeding fly ash in electric power plant |
| CN101503202A (en) * | 2009-02-11 | 2009-08-12 | 陕西理工学院 | Technique for hydro-thermal synthesis of high purity zeolite and fly ash zeolite adsorbing agent from fly ash |
| CN105253639A (en) * | 2015-10-15 | 2016-01-20 | 浙江工业大学 | Hydraulically-driven moving type spiral coal ash conveying device and operation method thereof |
| CN205139076U (en) * | 2015-11-20 | 2016-04-06 | 西安工业大学 | Full automatization water quality safety detection device based on intelligent machine arm |
| CN106495181A (en) * | 2016-10-26 | 2017-03-15 | 天津大学 | A kind of method that flyash synthesizes y-type zeolite |
| CN106865565A (en) * | 2017-03-26 | 2017-06-20 | 天津大学 | A kind of flyash synthesizes the method for X-type zeolite |
| CN109055957A (en) * | 2018-08-28 | 2018-12-21 | 格林美（武汉）城市矿产循环产业园开发有限公司 | A kind of intelligence pickling system |
| CN111068612A (en) * | 2019-12-31 | 2020-04-28 | 中国建筑材料科学研究总院有限公司 | Method for preparing zeolite-like porous material by using solid waste, zeolite-like porous material and application thereof |
| CN112263890A (en) * | 2020-09-10 | 2021-01-26 | 国电新能源技术研究院有限公司 | Flue gas waste heat utilization type carbon capture method and system |
| CN113005466A (en) * | 2021-03-24 | 2021-06-22 | 广东邦普循环科技有限公司 | Safe pickling equipment and method |
| CN113144818A (en) * | 2021-04-29 | 2021-07-23 | 华电宁夏灵武发电有限公司 | Fly ash-based carbon dioxide absorption system and fly ash recycling method for absorbing carbon dioxide |
| CN113353949A (en) * | 2021-06-30 | 2021-09-07 | 东北大学 | Synthetic zeolite of fly ash and coal gangue aluminum extraction slag and comprehensive utilization method thereof |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2023226473A1 (en) * | 2022-05-23 | 2023-11-30 | 中国华能集团清洁能源技术研究院有限公司 | Cooperative utilization system for coal gangue power generation and co2 mineralization and working method |
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