CN103861446B - Flue gas CO2With ardealite serous coat three-phase fluidization mineralization methods - Google Patents
Flue gas CO2With ardealite serous coat three-phase fluidization mineralization methods Download PDFInfo
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- CN103861446B CN103861446B CN201410124933.1A CN201410124933A CN103861446B CN 103861446 B CN103861446 B CN 103861446B CN 201410124933 A CN201410124933 A CN 201410124933A CN 103861446 B CN103861446 B CN 103861446B
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 22
- 239000003546 flue gas Substances 0.000 title claims abstract description 22
- 238000000034 method Methods 0.000 title claims abstract description 22
- 238000005243 fluidization Methods 0.000 title claims abstract description 19
- 230000033558 biomineral tissue development Effects 0.000 title claims description 5
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 81
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 39
- 239000007789 gas Substances 0.000 claims abstract description 33
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 claims abstract description 32
- 229910000069 nitrogen hydride Inorganic materials 0.000 claims abstract description 20
- 229910000019 calcium carbonate Inorganic materials 0.000 claims abstract description 16
- 230000004087 circulation Effects 0.000 claims abstract description 14
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 claims abstract description 7
- 229910052921 ammonium sulfate Inorganic materials 0.000 claims abstract description 7
- 235000011130 ammonium sulphate Nutrition 0.000 claims abstract description 7
- 239000011324 bead Substances 0.000 claims abstract description 5
- 239000007787 solid Substances 0.000 claims abstract description 5
- 239000002002 slurry Substances 0.000 claims description 44
- 238000006243 chemical reaction Methods 0.000 claims description 32
- 238000002425 crystallisation Methods 0.000 claims description 14
- 239000013505 freshwater Substances 0.000 claims description 14
- 230000008025 crystallization Effects 0.000 claims description 13
- 239000008246 gaseous mixture Substances 0.000 claims description 9
- 229910052602 gypsum Inorganic materials 0.000 claims description 8
- 239000002245 particle Substances 0.000 claims description 5
- 239000008187 granular material Substances 0.000 claims description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 3
- 229910052799 carbon Inorganic materials 0.000 claims description 3
- 238000001816 cooling Methods 0.000 claims description 3
- 239000004744 fabric Substances 0.000 claims description 3
- 239000003595 mist Substances 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims description 3
- 238000011084 recovery Methods 0.000 claims description 3
- 230000009467 reduction Effects 0.000 claims description 3
- 230000004044 response Effects 0.000 claims description 2
- 235000010216 calcium carbonate Nutrition 0.000 abstract description 12
- PASHVRUKOFIRIK-UHFFFAOYSA-L calcium sulfate dihydrate Chemical compound O.O.[Ca+2].[O-]S([O-])(=O)=O PASHVRUKOFIRIK-UHFFFAOYSA-L 0.000 abstract description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 3
- 238000010521 absorption reaction Methods 0.000 abstract description 2
- 239000012530 fluid Substances 0.000 abstract description 2
- 239000007788 liquid Substances 0.000 abstract description 2
- 239000011859 microparticle Substances 0.000 abstract 1
- 230000001052 transient effect Effects 0.000 abstract 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 27
- 239000012071 phase Substances 0.000 description 18
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 8
- 230000005540 biological transmission Effects 0.000 description 5
- 239000004570 mortar (masonry) Substances 0.000 description 5
- 230000008569 process Effects 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 4
- 238000007599 discharging Methods 0.000 description 3
- 230000002745 absorbent Effects 0.000 description 2
- 239000002250 absorbent Substances 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 238000011143 downstream manufacturing Methods 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000000725 suspension Substances 0.000 description 2
- 239000004743 Polypropylene Substances 0.000 description 1
- BIGPRXCJEDHCLP-UHFFFAOYSA-N ammonium bisulfate Chemical compound [NH4+].OS([O-])(=O)=O BIGPRXCJEDHCLP-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 230000009615 deamination Effects 0.000 description 1
- 238000006481 deamination reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000003792 electrolyte Substances 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 230000004907 flux Effects 0.000 description 1
- 238000007710 freezing Methods 0.000 description 1
- 230000008014 freezing Effects 0.000 description 1
- XLYOFNOQVPJJNP-ZSJDYOACSA-N heavy water Substances [2H]O[2H] XLYOFNOQVPJJNP-ZSJDYOACSA-N 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 239000011268 mixed slurry Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 235000011837 pasties Nutrition 0.000 description 1
- -1 polypropylene Polymers 0.000 description 1
- 229920001155 polypropylene Polymers 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000004537 pulping Methods 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 238000012216 screening Methods 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 238000003746 solid phase reaction Methods 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
Landscapes
- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
Abstract
A kind of flue gas CO2Does flue gas mix by double-deck gas-liquid-solid serous coat reactor with ammonia, the wherein uniform ardealite serous coat of the bead surface of turbulence, specific surface area 150 ~ 600 with the method for ardealite serous coat three-phase fluidization mineralising m-1, thickness 80 ~ 800 microns, phosphogypsum and calcium carbonate microparticle, react 2NH with air-flow3+ CO2+ SO4 2-+ Ca2++ H2O = CaCO3 ↓+ 2NH4 ++ SO4 2-Reduce NH3And CO2Equilibrium partial pressure, improves gas-liquid mass transfer motive force. Reclaiming tail gas ammonia with the double-deck serous coat three-phase fluid bed reactor of similar structures, ardealite and water are made into the ammonia that size circulations makes the sulfate radical molar flow of dissolving exceed in tail gas, and ammonia is by serosa surface transient absorption. Implement this method more than 80% CO2Mineralising is that calcium carbonate, more than 96% ardealite are converted into ammonium sulfate, and room temperature emission containing ammonia lower than 10 ppm.
Description
Technical fieldThe present invention relates to smoke carbon dioxide reduction of discharging, the utilization of Industrial Solid Waste ardealite and ammonia-containing exhaust processing technology field, the ardealite serous coat three-phase fluidization mineralising co-producing calcium carbonate of particularly three's coupling and the method for ammonium sulfate.
Background technologyProcess industrial discharges a large amount of flue gas CO2, cause greenhouse effect and atmospheric pollution. CO2Trap, seal up for safekeeping and utilize (CCSU) that source can be realized to reduce discharging. The various methods implementing CCSU, all flue gas CO2Trapping is as independent link. Flue gas flow is big, CO2Content is low, though existing chemical absorption method arresting efficiency is high but energy consumption, absorbent consumption and tail gas secondary pollution problems wait solution. It is reported that most emulative ammonia process traps coal fired power generation flue gas CO2, only namely absorbent regeneration needs to consume heat energy (ZhangM, the GuoY.RatebasedmodelingofabsorptionandregenerationforCO suitable with generated energy2capturebyaqueousammoniasolution[J],AppliedEnergy, 2013,111:142-152). Another kind has the ammonia flue gas CO of desulphurization denitration function concurrently2Trapping technique (ECO2) cost is 40 dollars/t-CO2(PowerspanAnnouncesResultsofIndependentAssessmentofItsCO2CaptureTechnology, www.worleyparsons.com), but CO after trapping2Further handling problems still need to solve. In addition, lot of energy is also wanted in the control of tail gas ammonia content, such as freezing ammonia process technology is reach tail gas ammonia content < environmental protection standard of 10ppmv uses Refrigeration Technique that tail gas deamination system temperature is reduced to below 10F (MathiasPM, ReddyS, O ' ConnellJP.QuantitativeEvaluationoftheAqueousAmmoniaProce ssforCO2CaptureUsingFundamentalDataandThermodynamicAnalysis[J],EnergyProcedia, 2009,1:1227-1234). Another kind of method is to make containing CO2Gas and Gypsum Fibrosum ammonia suspension directly there is gas-liquid-solid phase reaction mass transfer, CO2Mineralising is precipitated as calcium carbonate coproduction of ammonia sulfate simultaneously, and (Liu Shan works as, Zhu Jiahua, and summer element is blue.The experimentation of Gypsum Fibrosum ammonia suspension absorbing carbon dioxide, Sichuan chemical industry, 2004, (3): 1 ~ 3), but flue gas CO2The direct contact reactor structure of-gypsum-ammonia-water three-phase and regulation and control method have no report.CO2-ammonia-water is Volatile Weak Electrolyte System solution, adds ardealite (CaSO4·2H2O) making airwater mist cooling thermodynamic equilibrium nature change, the structure of reactor adapted with it and regulation and control method are high effective flue gas CO2The core of mineralising and tail gas Ammonia recovery technology.
Summary of the inventionDisclosure one flue gas CO2With ardealite serous coat three-phase fluidization mineralization methods. Temperature 10 ~ 80 DEG C, CO2The flue gas of volumetric concentration 8 ~ 30% with by NH3/CO2The room temperature ammonia of mol ratio 1.55 ~ 1.90 proportioning forms gaseous mixture and enters ardealite serous coat three-phase fluidization mineralising reactor 1; from bottom to top through double-deck ardealite serous coat three phase fluidized bed; the hollow shell bead of diameter 6 ~ 25mm is suspended in air-flow turbulence; the uniform one layer of ardealite pasty film of bead surface; calcium carbonate and ardealite granulate mixture total volume concentration 5 ~ 15%, grain diameter 1 ~ 50 micron, thickness 80 ~ 800 microns in film; serous coat specific surface area 150 ~ 600(1/m), by serosa surface and the CO in mixed airflow2And NH3There is airwater mist cooling consecutive reaction
2NH3+CO2+SO4 2-+Ca2++H2O=CaCO3↓+2NH4 ++SO4 2-(1)
Thus reduce the free NH of liquid phase3And CO2Concentration, the NH according to Henry's law serosa surface3And CO2Equilibrium partial pressure all declines therewith, thus gas phase NH can reduced3And CO2Improve gas-liquid mass transfer motive force while dividing potential drop, make gaseous mixture pass through CO after lower floor's bed reacts2And NH3Content all reduces more than 80%, when entering upper bed containing NH3Lower than 2%(volume). Free NH in the serous coat of the new cloth of upper bed3And CO2Content is less, temperature is higher close to room temperature, absorbability, at free NH3Content is less than 0.01%(mass) under condition, after can making to be reacted by upper bed, gaseous mixture is containing NH3Lower than 0.8%(volume), containing CO2Lower than 4.0%(volume), the tail gas ammonia entering back into similar structures reclaims reactor 2, flow through double-deck ardealite serous coat three phase fluidized bed from the bottom up, the slurry being made into by the ardealite being newly added and fresh water (FW) is circulated by lower floor's bed, wherein exceedes tail gas containing ammonia molar flow containing the sulfate radical molar flow dissolved, furthermore tail gas remnants CO2Volumetric concentration, more than 2%, makes the reaction of recovery tail gas Ammonia can complete by (1) formula moment at serosa surface, and lower floor's bed outlet tail gas volumetric concentration containing ammonia, less than 10ppm, finally ascends into discharge after upper bed is purified by Fresh process moisture film.
Ardealite raw material is through screening without the granule more than 1mm or showy property impurity, calcium sulphate dihydrate (CaSO4·2H2O) content is not less than 92%(butt), feeding quantity presses CaSO4·2H2O/NH3Mol ratio 0.45 ~ 0.49 proportioning, is directly added into groove 4 with slurry; Amount of water presses H2O/NH3Mol ratio 5.0 ~ 6.0 proportioning, sprinkle adds tail gas ammonia and reclaims the upper bed top of reactor 2, groove 4 with slurry is entered after flowing through two-stage fluidized from top to bottom, with ardealite mixing pulping, mean residence time 15 ~ 25 minutes, slurry is pumped from trench bottom with slurry by pump for mortar transmission 10 metering, is divided into overflow and underflow by feeding swirler 7, the volume flow ratio 2 ~ 3 of overflow and underflow, overflow adds ardealite serous coat three-phase fluidization mineralising reactor 1 upper bed top containing solid particle volumetric concentration 2 ~ 10%, uniform sprinkle, and underflow is directly added into crystallization conversion device 3. Simultaneously, making the slurry in groove with slurry be reclaimed lower floor's bed circulation of reactor 2 by tail gas ammonia with circulating pump 9 with slurry by the overflow of cyclone 6 with slurry, circulation slurry volume flow is 8 ~ 10 times of amount of water, adds ardealite serous coat three-phase tail gas ammonia reclaim reactor 2 lower floor's bed top containing solid particle volumetric concentration 2 ~ 10%, uniform sprinkle.Above-mentioned with slurry and conveying, circulation operation carry out all at normal temperatures.
Add the ardealite slurry on ardealite serous coat three-phase fluidization mineralising reactor 1 upper bed top, after passing through two-stage fluidized and gaseous mixture countercurrent reaction, enter crystallization conversion device 3, wherein mean residence time 60 ~ 120 minutes, CaSO4·2H2O conversion ratio more than 96%, the calcium carbonate of generation and ammonium sulfate slurry are pumped by pump for mortar transmission 11 metering bottom crystallization conversion device, remove Downstream processing. Simultaneously, make slurry in crystallization conversion device by reacting the overflow of cyclone 5 in the bed circulation of ardealite serous coat three-phase fluidization mineralising reactor lower floor with reaction cycle pump 8, the volume flow of circulation slurry and upper bed drop the ratio of the volume flow of pouring be 5 ~ 10, containing solid particle volumetric concentration 2 ~ 10%. The slurry of circulation, by the outside output-response heat of cooler 12, enters cooler slurry temperature 65 ~ 80 DEG C, goes out cooler slurry temperature 60 ~ 70 DEG C, maintain crystallization conversion device 3 and operate temperature 65 ~ 80 DEG C.
This method result of implementation, be make more than 80% flue gas CO2Mineralising be calcium carbonate, more than 96% ardealite (CaSO4·2H2O) it is converted into ammonium sulfate, and exports ammonia and CO at 60 ~ 75 DEG C of warm areas2Reaction heat, room temperature emission of carbon reduce discharging tail gas volumetric concentration containing ammonia less than 10ppm.
Accompanying drawing explanationAccompanying drawing 1 is flue gas CO provided by the invention2With ardealite serous coat three-phase fluidization mineralization process schematic diagram. In figure: 1-ardealite serous coat three-phase fluidization mineralising reactor; 2-tail gas ammonia reclaims reactor; 3-crystallization conversion device; 4-groove with slurry; 5-reacts cyclone; 6-cyclone with slurry; 7-feeds in raw material cyclone; 8-reaction cycle pump; 9-circulating pump with slurry; 10,11-pump for mortar transmission; 12-cooler.
Detailed description of the inventionBelow in conjunction with but be not limited to embodiment set forth the specific embodiment of the invention
Logistics: CO2Volumetric concentration 14%(butt) flue gas 50000Nm3/ h, temperature 80 DEG C, pressure 125kPa(is exhausted); NH3Gas 550kmol/h, pressure 150kPa(is exhausted); Ardealite 50000kg/h(butt), CaSO4·2H2O content is not less than 92%(butt); Fresh water (FW), 48800kg/h. Except indicating temperature, above logistics is room temperature.
Flue gas and ammonia are mixed into ardealite serous coat three-phase fluidization mineralising reactor 1, apparent volume flux 1.0m/s, flow through double-deck serous coat fluid bed from bottom to top, bed the serous coat thickness 80 ~ 800 microns of thin-walled polypropylene hollow ball surface distributed of interior diameter 15mm, intramembranous particles volumetric concentration about 10%, grain diameter 1 ~ 50 micron, serous coat and the CO in mixed airflow2And NH3Reaction generates precipitation of calcium carbonate and free NH4 +And SO4 2-, reaction temperature 60 ~ 75 DEG C, leave the air-flow CO at lower floor's bed top after reaction2Volumetric concentration about 4.0%, NH3Volumetric concentration about 1.8%, ascends into upper bed and continues reaction. Free NH in the serous coat of the new cloth of upper bed3Content is less than 0.01%(mass), leave the tail gas balance NH at upper bed top after reaction3Content is lower than 0.6%(volume), CO2Content is lower than 3.5%(volume), enter tail gas ammonia and reclaim the bottom of reactor 2, rise and flow through double-deck ardealite serous coat three phase fluidized bed, slurry is made into by the ardealite being newly added and fresh water (FW), by sulfate radical free in the slurry that lower floor's bed circulates more than 16kmol/h, absorb Ammonia in tail gas and make its residual ammonia content less than 10ppm(volume), remaining CO2Content is lower than 3.0%(volume), tail gas discharges after being purified by Fresh process moisture film finally by upper bed again.
Ardealite mixes in groove 4 with slurry with fresh water (FW), mean residence time 20 minutes.Make slurry reclaim circulation volume flow between reactor 2 lower floor's bed and groove with slurry at tail gas ammonia with circulating pump 9 with slurry by cyclone 6 with slurry overflow and reach 550m3/ h, pump for mortar transmission 10 the slurry volume flow carried to ardealite serous coat three-phase fluidization mineralising reactor 1 and crystallization conversion device 3 is about 70m3/ h, entering after crystallization conversion device 3 averaged residence 100 minutes wherein, calcium carbonate 26500kg/h and the ammonium sulfate 35000kg/h mixed slurry of generation are pumped Downstream processing by pump for mortar transmission 11. With reaction cycle pump 8 by cooler 12 and reaction cyclone 5 overflow, between lower floor's bed of crystallization conversion device 3 and ardealite serous coat three-phase fluidization mineralising reactor 1, set up size circulations, volume flow reaches 500m3/ h, slurry is into and out of the temperature respectively 72 DEG C, 65 DEG C of cooler 12. Crystallization conversion device operation temperature 70 ~ 75 DEG C.
Embodiment illustrates the invention has the beneficial effects as follows and makes (80 DEG C) flue gas (50000Nm3/ h) in CO2(7000Nm3/ h) 85% it is mineralized as calcium carbonate product (26500kg/h), the CaSO in ardealite (50000kg/h)4·2H2O conversion ratio reaches more than 96% (obtaining ammonium sulfate product 35000kg/h), after carbon emission reduction tail gas containing ammonia less than 10ppmv. The Lowlevel thermal energy 6.5MW of exportable 60 ~ 70 DEG C simultaneously.
The invention is not restricted to above-described embodiment, its technical scheme is explained at Summary.
Claims (2)
1. a flue gas CO2With ardealite serous coat three-phase fluidization mineralization methods; it is characterized in that the three-phase fluidization mineralising reactor that the gaseous mixture that flue gas and ammonia are formed is constituted from bottom to top through double-deck ardealite serous coat three phase fluidized bed; the uniform one layer of ardealite serous coat of hollow shell bead surface being suspended in air-flow turbulence; calcium carbonate and ardealite granulate mixture total volume concentration 5～15%, grain diameter 1～50 micron, thickness 80～800 microns, serous coat specific surface area 150～600m in film-1, by film surface and the CO in air-flow2And NH3There is airwater mist cooling consecutive reaction
2NH3+CO2+SO4 2-+Ca2++H2O=CaCO3↓+2NH4 ++SO4 2-
Gaseous mixture is made to pass through CO after lower floor's bed reacts2And NH3Content reduces more than 80%, NH3Volume content lower than 2%; Free NH in the serous coat of the new cloth of upper bed3When mass concentration is less than 0.01%, after being reacted by upper bed, gaseous mixture is containing NH3Volume content is lower than 0.8%;
Flue-gas temperature 10～80 DEG C, CO2Volumetric concentration 8～30%, gaseous mixture proportioning ammonia presses NH3/CO2Mol ratio 1.55～1.90;
The proportioning of ardealite slurry, by CaSO4·2H2O/NH3Mol ratio 0.45～0.49, H2O/NH3Mol ratio 5.0～6.0;
Ardealite slurry was groove mean residence time with slurry 15～25 minutes, overflow and underflow it is classified as with cyclone, underflow is directly added into crystallization conversion device, the volume flow of overflow is 2～3 times of underflow, add the ardealite serous coat three phase fluidized bed top, upper strata of three-phase fluidization mineralising reactor containing solid particle volumetric concentration 2～10%, uniform sprinkle, crystallization conversion device is entered after passing through double-deck ardealite serous coat three phase fluidized bed and gaseous mixture countercurrent reaction, mean residence time 60～120 minutes wherein, make the flue gas CO of more than 80%2Mineralising be calcium carbonate, more than 96% ardealite CaSO4·2H2O is converted into ammonium sulfate;
The lower floor's ardealite serous coat three phase fluidized bed circulation by three-phase fluidization mineralising reactor of the slurry in crystallization conversion device, the ratio of the volume flow that the volume flow of circulation slurry drops pouring with upper bed is 5～10;
Circulation slurry, by the outside output-response heat of cooler, enters cooler slurry temperature 65～80 DEG C, goes out cooler slurry temperature 60～70 DEG C, maintains crystallization conversion device operation temperature 65～80 DEG C.
2. the method reclaiming tail gas Ammonia, it is characterised in that the tail gas after carbon emission reduction is containing NH3Volumetric concentration is lower than 0.8%, containing CO2Volumetric concentration is lower than 4.0%; flow through the tail gas ammonia recovery reactor that double-deck ardealite serous coat three phase fluidized bed is constituted from the bottom up; the uniform one layer of ardealite serous coat of hollow shell bead surface being suspended in air-flow turbulence; calcium carbonate and ardealite granulate mixture total volume concentration 5～15%, grain diameter 1～50 micron, thickness 80～800 microns, serous coat specific surface area 150～600m in film-1, complete to reclaim the reaction of tail gas Ammonia in lower floor's bed serosa surface moment, make to export tail gas volumetric concentration containing ammonia under room temperature less than 10ppm;
Being made into ardealite slurry by ardealite and fresh water (FW), ardealite is directly added into groove with slurry, and the ardealite serous coat three phase fluidized bed top, upper strata that fresh water (FW) reclaims reactor from tail gas ammonia adds, and enters groove with slurry after flowing through bunk beds from top to bottom;
The lower floor's ardealite serous coat three phase fluidized bed circulation by three-phase fluidization mineralising reactor of the slurry in groove with slurry, the volume flow of circulation slurry is 8～10 times of fresh water (FW) volume flow, wherein exceedes tail gas containing ammonia molar flow containing the sulfate radical molar flow dissolved.
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| RU2782927C1 (en) * | 2022-01-14 | 2022-11-07 | Самуил Вульфович Гольверк | Method for lime purification of flue gases of coal-fired boilers of tpps from carbon dioxide |
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| CA3011636C (en) * | 2016-01-21 | 2023-10-31 | Squaretail Pty Ltd | Method and apparatus for removing carbon dioxide from flue gas |
| CN106925118A (en) * | 2017-03-20 | 2017-07-07 | 南京师范大学 | CO in a kind of power plant using the desulfurated plaster not being dehydrated removing2Apparatus and method |
| CN107445190A (en) * | 2017-09-30 | 2017-12-08 | 广西华洋矿源材料有限公司 | A kind of method that high-quality superfine light calcium carbonate is prepared using gypsum as raw material |
| CN107698008A (en) * | 2017-11-25 | 2018-02-16 | 山西师范大学 | New application of the solid-state ammonium sulfate calcium carbonate reaction in water body NH_3-N treating |
| CN108889251B (en) * | 2018-08-20 | 2023-09-29 | 中国华能集团有限公司 | Entrained-flow bed device and method for humidifying and mineralizing carbon dioxide |
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| CN102836627A (en) * | 2012-07-02 | 2012-12-26 | 四川大学 | One-step process energy-saving and water-saving cleaning technology for converting smoke carbon dioxide into ardealite |
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| US8231850B2 (en) * | 2010-06-08 | 2012-07-31 | Korea Institute Of Geoscience And Mineral Resources | Economical sequestration of carbon dioxide by the mixed gas |
| CN102671529A (en) * | 2012-06-04 | 2012-09-19 | 四川大学 | Method for co-producing sulfur-based compound fertilizer through coupling desulfurization, denitration and decarbonization of flue gas with ardealite transformation |
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