CN115228278B - PH value regulated calcium carbonate for accelerating mineralization and absorption of CO in flue gas2Systems and methods of (1) - Google Patents
PH value regulated calcium carbonate for accelerating mineralization and absorption of CO in flue gas2Systems and methods of (1) Download PDFInfo
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- 230000033558 biomineral tissue development Effects 0.000 title claims abstract description 191
- 238000010521 absorption reaction Methods 0.000 title claims abstract description 80
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 title claims abstract description 58
- 238000000034 method Methods 0.000 title claims abstract description 43
- 229910000019 calcium carbonate Inorganic materials 0.000 title claims abstract description 28
- 230000001105 regulatory effect Effects 0.000 title claims abstract description 19
- 239000004568 cement Substances 0.000 claims abstract description 120
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 74
- 238000003756 stirring Methods 0.000 claims abstract description 67
- 239000002912 waste gas Substances 0.000 claims abstract description 65
- 238000003860 storage Methods 0.000 claims abstract description 46
- VMHLLURERBWHNL-UHFFFAOYSA-M Sodium acetate Chemical compound [Na+].CC([O-])=O VMHLLURERBWHNL-UHFFFAOYSA-M 0.000 claims abstract description 26
- 239000001632 sodium acetate Substances 0.000 claims abstract description 26
- 235000017281 sodium acetate Nutrition 0.000 claims abstract description 26
- 238000001514 detection method Methods 0.000 claims abstract description 23
- 239000000654 additive Substances 0.000 claims abstract description 20
- 230000000996 additive effect Effects 0.000 claims abstract description 20
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 18
- 238000005261 decarburization Methods 0.000 claims abstract description 18
- 239000003546 flue gas Substances 0.000 claims abstract description 18
- 239000007864 aqueous solution Substances 0.000 claims abstract description 14
- 239000000463 material Substances 0.000 claims description 27
- 230000001089 mineralizing effect Effects 0.000 claims description 15
- 238000005070 sampling Methods 0.000 claims description 14
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 10
- 239000000920 calcium hydroxide Substances 0.000 claims description 10
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims description 10
- 239000000292 calcium oxide Substances 0.000 claims description 10
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 claims description 10
- 230000001276 controlling effect Effects 0.000 claims description 9
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 claims description 7
- 238000012544 monitoring process Methods 0.000 claims description 4
- 239000000779 smoke Substances 0.000 claims description 4
- 238000007711 solidification Methods 0.000 claims description 4
- 230000008023 solidification Effects 0.000 claims description 4
- 241000537371 Fraxinus caroliniana Species 0.000 claims description 3
- 235000010891 Ptelea trifoliata Nutrition 0.000 claims description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 abstract description 99
- 229910002092 carbon dioxide Inorganic materials 0.000 abstract description 50
- 239000001569 carbon dioxide Substances 0.000 abstract description 49
- 238000006243 chemical reaction Methods 0.000 abstract description 16
- 239000013078 crystal Substances 0.000 abstract description 5
- 239000002245 particle Substances 0.000 description 13
- 239000000460 chlorine Substances 0.000 description 6
- 229910052801 chlorine Inorganic materials 0.000 description 6
- 230000000052 comparative effect Effects 0.000 description 6
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 5
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 5
- 239000002910 solid waste Substances 0.000 description 5
- 239000011593 sulfur Substances 0.000 description 5
- 229910052717 sulfur Inorganic materials 0.000 description 5
- 239000003513 alkali Substances 0.000 description 4
- 239000000428 dust Substances 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000000395 magnesium oxide Substances 0.000 description 3
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 2
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 2
- 241000196324 Embryophyta Species 0.000 description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 238000003825 pressing Methods 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- 239000010802 sludge Substances 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 238000009423 ventilation Methods 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- KKCBUQHMOMHUOY-UHFFFAOYSA-N Na2O Inorganic materials [O-2].[Na+].[Na+] KKCBUQHMOMHUOY-UHFFFAOYSA-N 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 229910052681 coesite Inorganic materials 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 229910052593 corundum Inorganic materials 0.000 description 1
- 229910052906 cristobalite Inorganic materials 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000010791 domestic waste Substances 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 description 1
- JEIPFZHSYJVQDO-UHFFFAOYSA-N iron(III) oxide Inorganic materials O=[Fe]O[Fe]=O JEIPFZHSYJVQDO-UHFFFAOYSA-N 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000010813 municipal solid waste Substances 0.000 description 1
- 230000008092 positive effect Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 229910052682 stishovite Inorganic materials 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 229910052905 tridymite Inorganic materials 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 229910001845 yogo sapphire Inorganic materials 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/80—Semi-solid phase processes, i.e. by using slurries
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/62—Carbon oxides
-
- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
The invention discloses a system and a method for accelerating mineralization and absorption of CO 2 in flue gas by using pH value regulated calcium carbonate, wherein the system comprises a cement kiln bypass blow-down ash storage, metering and conveying system, an additive system, a water supply system, a kiln tail waste gas air supply system, a pH online detection system, a stirring mineralization absorption system, a decarburization waste gas air-out system and a mineralization ash conveying system; in the mineralization process, sodium acetate is added, the mass fraction of sodium acetate aqueous solution is controlled to be 1-3%, water is added into bypass air-release ash of a cement kiln according to the proportion of 0.1-0.3 for stirring, meanwhile, the pH value is regulated and controlled within the range of 10-11, the size of calcium carbonate crystals generated by the reaction is regulated, and the mineralization reaction rate and mineralization absorption are accelerated. The invention can realize that the absorption rate of carbon dioxide in kiln tail waste gas reaches more than 30 percent, develops a new way for reducing the carbon dioxide emission of cement factories, and has wide practical application and popularization value.
Description
Technical Field
The invention relates to the technical field of reducing carbon dioxide emission in the cement industry, in particular to a system and a method for accelerating mineralization and absorption of CO 2 in flue gas by using pH value regulated calcium carbonate.
Background
It is counted that carbon dioxide discharged from global cement production accounts for 7% of the total carbon dioxide discharge, and the cement industry greatly reduces carbon dioxide discharge and is expected to reduce adverse effects on climate warming. The cement industry is also a large household of carbon dioxide emission in China, and the data show that the total annual emission amount of carbon dioxide in China in 2019 is about 100 hundred million tons, and the annual emission amount of carbon dioxide in the world is 30%, wherein the emission amount of the carbon dioxide in the cement industry is about 13.2 hundred million tons, and the total emission amount of carbon dioxide in industrial enterprises in China is about 15%, so that the carbon dioxide emission reduction task in the cement industry is difficult.
The mineralization and absorption of carbon dioxide have the characteristics of small environmental risk, no need of monitoring, and the generated carbonate can naturally and stably exist for a long time, and is expected to become an important mode for carbon dioxide emission reduction and resource utilization. The method can discharge a large amount of solid waste containing calcium and magnesium oxide or hydroxide each year in China, can be used for mineralizing and absorbing carbon dioxide, and has the advantages of wide source, large total solid carbon amount, suitability for local material taking and the like. Therefore, one of the methods for reducing carbon dioxide emission in the cement industry is to react the generated carbon dioxide with alkaline materials generated in the cement manufacturing process to form carbonate, thereby realizing permanent carbon fixation and contributing to carbon emission reduction in the cement industry.
The cement kiln bypass air-release dust collection ash is a calcium-containing alkaline material discharged by a bypass air-release system in the cement production process. Because the cement kiln is used for cooperatively disposing garbage, sludge and solid waste, the components are complex, the sulfur and chlorine content is high, and a large amount of alkali, chlorine and sulfur elements are released in the cement kiln cooperative disposal process and are circularly enriched in the kiln, the skinning and blockage in the kiln are easy to cause. In order to avoid the cyclic enrichment of alkali, chlorine and sulfur in a kiln system, when the sulfur and chlorine content in the hot raw material reaches a certain value, a bypass ventilation technology is adopted to release a part of flue gas enriched with high-concentration alkali, chlorine and sulfur so as to alleviate the problem; the partial calcium oxide and magnesium oxide which are released together with the flue gas and a large amount of alkaline substances are also released, so that bypass air release dust collection ash is a high-alkali high-chlorine material with complex components, and the main utilization mode is to add the bypass air release dust collection ash into cement in a small amount as a mixed material at present. With the increasing consumption of municipal domestic waste, sludge, solid waste and dangerous waste in the cement industry of China, a large number of cement factories build a cooperative disposal system, a bypass air release system gradually becomes a standard of a cement kiln for cooperatively disposing solid waste water, the generation amount of bypass air release dust collection ash is increased year by year, and the comprehensive utilization difficulty is increased.
The mineralization of the bypass air-release dust-collecting ash of the cement plant to absorb the carbon dioxide in the kiln tail waste gas discharged by the cement plant is an important way for utilizing the bypass air-release dust-collecting ash with high added value, but because the bypass air-release dust-collecting ash is in the process of absorbing the carbon dioxide in the kiln tail waste gas, the generated calcium carbonate crystal can be deposited on the surface of the bypass air-release dust-collecting ash particles, thereby delaying the mineralization absorption reaction efficiency of the carbon dioxide.
Disclosure of Invention
The invention provides a system and a method for accelerating mineralization and absorption of CO 2 in flue gas by using pH value regulated calcium carbonate to solve the problems in the prior art.
The system for accelerating mineralization and absorption of CO 2 in flue gas by using the pH value regulated calcium carbonate comprises a cement kiln bypass blow-down ash storage, metering and conveying system, an additive system, a water supply system, a kiln tail waste gas air supply system, a pH online detection system, a stirring mineralization absorption system, a decarburization waste gas air outlet system and a mineralization ash conveying system;
The outlet of the cement kiln bypass air-release ash storage, metering and conveying system is connected with the feed inlet of the stirring mineralization absorption system, the outlet of the additive system is connected with the inlet of the water supply system, the outlet of the water supply system is connected with the water inlet of the stirring mineralization absorption system, the outlet of the kiln tail waste gas air supply system is connected with the air inlet of the stirring mineralization absorption system, the pH on-line detection system is connected with the pH value sampling port of the stirring mineralization absorption system, the air outlet of the stirring mineralization absorption system is connected with the decarburization waste gas air outlet system, and the discharge port of the stirring mineralization absorption system is connected with the mineralization ash conveying system.
Preferably, the cement kiln bypass blow-down ash storage, metering and conveying system comprises a cement kiln bypass blow-down ash storage bin, an electric gate valve and a screw metering feeder which are sequentially connected, wherein an outlet of the screw metering feeder is connected with a feed inlet of the stirring mineralization absorption system.
Preferably, the additive system comprises an additive warehouse, a disc feeder and a feeding chute which are sequentially connected, wherein the outlet of the feeding chute is connected with the inlet of the water supply system.
Preferably, the water supply system comprises a water storage tank, a metering water pump and a water supply pipeline which are sequentially connected, and an outlet of the water supply pipeline is connected with a water inlet of the stirring mineralization absorption system.
Preferably, the stirring mineralization absorption system comprises a mineralization stirrer, and a feed inlet, a water inlet, a pH value sampling port, an air inlet, an air outlet and a discharge port which are positioned on the mineralization stirrer.
Preferably, the kiln tail waste gas air supply system comprises a centrifugal fan and a kiln tail waste gas air supply pipeline, wherein an inlet of the centrifugal fan is connected with a kiln tail chimney, and an outlet of the centrifugal fan is connected with an air inlet of the stirring mineralization absorption system through the kiln tail waste gas air supply pipeline; the decarburization waste gas air-out system comprises a decarburization waste gas air-out pipeline, an air outlet of the stirring mineralization absorption system is connected with an inlet of the decarburization waste gas air-out pipeline, and an outlet of the decarburization waste gas air-out pipeline is connected with a kiln tail chimney.
Preferably, the pH on-line detection system comprises a sampling device and a detection device, wherein the sampling device is arranged at a pH value sampling port of the mineralization stirrer.
A method for accelerating mineralization and absorption of CO 2 in flue gas by using pH value regulated calcium carbonate, which utilizes the system to mineralize and absorb carbon dioxide comprises the following steps:
S1, adding sodium acetate into a water supply system through an additive system, and controlling the mass fraction of a sodium acetate aqueous solution to be 1-3%;
S2, feeding cement kiln bypass blow-off ash into a stirring mineralization absorption system through a cement kiln bypass blow-off ash storage, metering and conveying system, adding water according to the water-ash ratio of 0.1-0.3, and stirring for a certain time to enable calcium oxide in the cement kiln bypass blow-off ash to be fully hydrated into calcium hydroxide;
S3, diversion of mud kiln tail waste gas from a kiln tail chimney by a kiln tail waste gas air supply system, and feeding into a stirring mineralization absorption system according to the air volume of 3000-5000Nm 3/h, and feeding cement kiln tail waste gas while stirring, mineralizing for 0.5-1.5h, so that CO 2 in the cement kiln tail waste gas is absorbed by cement kiln bypass air release ash to realize permanent solidification;
s4, in the mineralization process, a pH value online detection system is used for monitoring the pH value of the materials in the stirring mineralization absorption system in the whole process, the pH value is ensured to be between 10 and 11, when the pH value is reduced to be less than 10, cement kiln bypass air release ash is slowly added into the stirring mineralization absorption system, and the pH value of the materials is maintained to be between 10 and 11 all the time until mineralization is completed;
S5, after mineralization is completed, stopping introducing waste gas at the tail of the cement kiln, opening a discharge opening of a stirring mineralization absorption system, and transporting the generated mineralized ash to a storage yard or a storage warehouse through a mineralized ash conveying system.
The invention has the advantages and positive effects that:
1. The invention provides a system and a method for accelerating mineralization and absorption of CO 2 in flue gas by adopting pH value to regulate and control calcium carbonate for the first time, and the technology can accelerate the solidification rate of carbon dioxide, improve the mineralization and absorption amount of carbon dioxide and has important significance for the practice of reducing the emission of carbon dioxide of cement factories;
2. In the sodium acetate environment, the pH value is regulated within the range of 10-11, so that calcium carbonate crystals can be promoted to grow continuously, and carbon dioxide can enter bypass ash particles through gaps among the calcium carbonate crystals to be mineralized continuously, thereby obviously accelerating the mineralization rate;
3. the mineralization absorption method is a semi-dry method, has simple process flow, is environment-friendly, and has no wastewater discharge;
4. the invention provides a new method for accelerating the mineralization and utilization of carbon dioxide in the cement industry, and opens up a new emission reduction path for the cement industry which is difficult to reduce emission; along with the increase of the alternative fuel and solid waste disposal demand in the cement industry, the bypass blow-off ash output is increased, and the method is suitable for large-area popularization and application and has good popularization and application prospects.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings that are needed in the description of the embodiments will be briefly described below, and it is obvious that the drawings in the following description are some embodiments of the present invention, and other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
FIG. 1 is a flow chart of a system for accelerating mineralization and absorption of CO 2 in flue gas by using pH value regulated calcium carbonate according to an embodiment of the present invention;
FIG. 2 is a schematic diagram of the mineralization reaction according to the present invention.
Detailed Description
The following description of the embodiments of the present invention will be made apparent and fully in view of the accompanying drawings, in which some, but not all embodiments of the invention are shown. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.
In the description of the present invention, it should be noted that, unless explicitly specified and limited otherwise, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be either fixedly connected, detachably connected, or integrally connected, for example; can be mechanically or electrically connected; can be directly connected or indirectly connected through an intermediate medium, and can be communication between two elements. The specific meaning of the above terms in the present invention will be understood in specific cases by those of ordinary skill in the art.
The traditional slurry absorption tower type mineralization process route has complex flow, a large amount of water is consumed, mineralized materials are subjected to filter pressing dehydration, and the filter pressing liquid contains a large amount of salt, so that high-salt wastewater which is difficult to treat is formed. The inventor develops a semi-dry mineralization technical route by optimizing the water addition amount, the ventilation amount and the mineralization time on the basis of a large number of tests, and combines the pH value regulation and control technology for accelerating the mineralization rate, thereby realizing the technical scheme of high mineralization rate, high mineralization degree and simple process flow of bypass blow-off ash.
Referring to fig. 1, an embodiment of the invention provides a system for accelerating mineralization and absorption of CO 2 in flue gas by using pH-regulated calcium carbonate, which comprises a cement kiln bypass blow-down ash storage, metering and conveying system, an additive system, a water supply system, a kiln tail waste gas air supply system, a pH online detection system, a stirring mineralization absorption system, a decarburization waste gas air-out system and a mineralization ash conveying system.
The stirring mineralization absorption system comprises a mineralization stirrer, a feed inlet, a water inlet, a pH value sampling port, an air inlet, an air outlet and a discharge port which are positioned on the mineralization stirrer.
The cement kiln bypass air-release ash storage, metering and conveying system comprises a cement kiln bypass air-release ash storage bin, an electric gate valve and a screw metering feeder which are sequentially connected, wherein an outlet of the screw metering feeder is connected with a feed inlet of the mineralizing mixer.
The additive system comprises an additive storage bin, a disc feeder and a feeding slide carriage which are sequentially connected, the water supply system comprises a water storage tank, a metering water pump and a water supply pipeline which are sequentially connected, an outlet of the feeding slide carriage is connected with an inlet of the water storage tank, and an outlet of the water supply pipeline is connected with a water inlet of the mineralizing mixer.
The pH on-line detection system comprises a sampling device and a detection device, wherein the sampling device is arranged at a pH value sampling port of the mineralization stirrer.
The kiln tail waste gas air supply system comprises a centrifugal fan and a kiln tail waste gas air supply pipeline, wherein an inlet of the centrifugal fan is connected with a kiln tail chimney, and an outlet of the centrifugal fan is connected with an air inlet of the mineralization mixer through the kiln tail waste gas air supply pipeline; the decarburization waste gas air-out system comprises a decarburization waste gas air-out pipeline, an air outlet of the mineralization stirrer is connected with an inlet of the decarburization waste gas air-out pipeline, and an outlet of the decarburization waste gas air-out pipeline is connected with a kiln tail chimney.
The discharge opening of the mineralization stirrer is connected with a mineralization ash conveying system.
A method for accelerating mineralization and absorption of CO 2 in flue gas by using pH value regulated calcium carbonate, which utilizes the system to mineralize and absorb carbon dioxide comprises the following steps:
s1, adding sodium acetate into a water storage tank through an additive system, and controlling the mass fraction of a sodium acetate aqueous solution to be 1-3%;
S2, feeding cement kiln bypass blow-off ash into a mineralization stirrer through a cement kiln bypass blow-off ash storage, metering and conveying system, adding water according to the water-ash ratio of 0.1-0.3, and stirring for 5-10 minutes, so that calcium oxide in the cement kiln bypass blow-off ash is fully hydrated into calcium hydroxide;
S3, diversion of tail waste gas of the kiln from a kiln tail chimney by a centrifugal fan, and feeding into a mineralization stirrer according to the air volume of 3000-5000Nm 3/h, and feeding the tail waste gas of the cement kiln while stirring, mineralizing for 0.5-1.5h, so that CO 2 in the tail waste gas of the cement kiln is absorbed by bypass blow-off ash of the cement kiln to realize permanent solidification;
S4, in the mineralization process, a pH value online detection system is used for monitoring the pH value of the materials in the mineralization stirrer in the whole process, the pH value is ensured to be between 10 and 11, when the pH value is reduced to be less than 10, cement kiln bypass blast ash is slowly added into the mineralization stirrer, and the pH value of the materials is maintained to be between 10 and 11 all the time until mineralization is completed;
S5, after mineralization is completed, stopping introducing waste gas at the tail of the cement kiln, opening a discharge opening of a mineralization stirrer, and transporting the generated mineralized ash to a storage yard or a warehouse through a mineralized ash conveying system.
The inventor researches and discovers that the reaction rate of mineralizing and absorbing carbon dioxide by using cement kiln bypass blow-off ash is influenced by the mineralization degree, caCO 3 particles generated by the reaction are covered on the surfaces of the bypass blow-off ash particles along with the increase of the mineralization degree, so that the carbon dioxide is prevented from further entering the particles to carry out mineralization reaction, and the reaction rate and the reaction degree are limited.
After the bypass air ash particles encounter water, calcium oxide in the bypass air ash particles reacts with the water to generate calcium hydroxide, and the calcium hydroxide reacts with CO 2 in kiln tail waste gas to generate calcium carbonate, which is shown in chemical reaction equations (1) and (2).
CaO+H2O→Ca(OH)2 (1)
Ca(OH)2+CO2→CaCO3+H2O (2)
With the development of the reaction process, the content of calcium oxide in the bypass ash particles is gradually reduced, the inner core is contracted, calcium hydroxide generated by the reaction of the calcium oxide and water is covered on the outer layer of the particles, the mineralization reaction of carbon dioxide and calcium hydroxide also occurs on the surfaces of the bypass ash particles, the calcium carbonate particles generated by the reaction are fine and cover the surfaces of the bypass ash particles, and the entry of carbon dioxide and the progress of the mineralization reaction are blocked, as shown in figure 2.
A large number of experimental researches show that by introducing a certain amount of sodium acetate as buffer and controlling the pH value of the material within the range of 10-11, the crystal size of calcium carbonate particles generated by the reaction can be increased, so that carbon dioxide can enter the calcium hydroxide layer through the calcium carbonate layer and continue to mineralize, thereby accelerating the mineralization reaction process and mineralization absorption.
For a further understanding of the content, features and efficacy of the present invention, the following examples 1-5 and comparative examples 1-3 are presented to illustrate the technical effects of the practice of the present invention:
First, the chemical composition of cement kiln bypass blow-down ash used for detection and analysis is shown in the following table 1:
TABLE 1 chemical composition of cement kiln bypass blow-off ash
| L.O.I | SiO2 | Al2O3 | Fe2O3 | CaO | MgO | K2O | Na2O | SO3 | Cl- |
| 10.34 | 10.50 | 3.44 | 1.90 | 48.55 | 1.66 | 14.98 | 0.47 | 1.48 | 7.653 |
Bypass blast ash theoretical absorption carbon dioxide (%) =cao content×44/56= 48.55 ×44/56=38.1%.
Example 1
Adding sodium acetate into a water storage tank through an additive system, controlling the mass fraction of sodium acetate aqueous solution to be 3%, and conveying 1 ton of cement kiln bypass blow-down ash into a mineralization stirrer through a cement kiln bypass blow-down ash storage, metering and conveying system; then, according to the proportion of the water-cement ratio of 0.1, feeding the sodium acetate aqueous solution into a mineralization stirrer through a water supply system, starting the mineralization stirrer to stir for 5 minutes, introducing 3000Nm 3/h cement kiln tail waste gas from a kiln tail chimney into the mineralization stirrer through a centrifugal fan, mineralizing and stirring for 0.5 hour, detecting the pH value of the material through a pH value online detection system in the mineralization process, slowly adding cement kiln bypass vent ash into the mineralization stirrer, and maintaining the pH value of the material to be between 10 and 11 all the time until mineralization is completed; after mineralization, stopping introducing waste gas at the tail of the cement kiln and stirring, and enabling the generated mineralized ash to enter a mineralized ash conveying system through a discharge opening of a mineralization stirrer and be transported to a storage yard or a warehouse.
Carbon dioxide absorption (%) = (mineralized ash after mineralization-unmineralized cement kiln bypass blast ash entering a mineralization mixer-mineralized water weight)/cement kiln bypass blast ash entering a mineralization mixer x 100%, and the absorption of carbon dioxide is detected to be 32%.
Example 2
Adding sodium acetate into a water storage tank through an additive system, controlling the mass fraction of sodium acetate aqueous solution to be 2%, and conveying 1 ton of cement kiln bypass blow-down ash into a mineralization stirrer through a cement kiln bypass blow-down ash storage, metering and conveying system; then, according to the proportion of the water-cement ratio of 0.2, feeding the sodium acetate aqueous solution into a mineralization stirrer through a water supply system, starting the mineralization stirrer to stir for 8 minutes, introducing 4000Nm 3/h cement kiln tail waste gas from a kiln tail chimney into the mineralization stirrer through a centrifugal fan, mineralizing and stirring for 1.0 hour, detecting the pH value of the material through a pH value online detection system in the mineralization process, slowly adding cement kiln bypass vent ash into the mineralization stirrer, and maintaining the pH value of the material to be between 10 and 11 all the time until mineralization is completed; after mineralization, stopping the waste gas at the tail of the cement kiln and stirring, and enabling the generated mineralized ash to enter a mineralized ash conveying system through a discharge opening of a mineralized stirrer and be transported to a storage yard or a warehouse.
Carbon dioxide absorption (%) = (mineralized ash after mineralization-unmineralized cement kiln bypass blast ash entering a mineralization mixer-mineralized water weight)/cement kiln bypass blast ash entering a mineralization mixer x 100%, and the absorption of carbon dioxide is detected to be 30%.
Example 3
Adding sodium acetate into a water storage tank through an additive system, controlling the mass fraction of sodium acetate aqueous solution to be 3%, and conveying 1 ton of cement kiln bypass blow-down ash into a mineralization stirrer through a cement kiln bypass blow-down ash storage, metering and conveying system; then, according to the proportion of the water-cement ratio of 0.3, feeding the sodium acetate aqueous solution into a mineralization stirrer through a water supply system, starting the mineralization stirrer to stir for 10 minutes, then introducing 5000Nm 3/h cement kiln tail waste gas from a kiln tail chimney into the mineralization stirrer through a centrifugal fan, mineralizing and stirring for 1.5 hours, detecting the pH value of the material through a pH value online detection system in the mineralization process, slowly adding cement kiln bypass vent ash into the mineralization stirrer, and maintaining the pH value of the material to be between 10 and 11 all the time until mineralization is completed; after mineralization, stopping introducing waste gas at the tail of the cement kiln and stirring, and enabling the generated mineralized ash to enter a mineralized ash conveying system through a discharge opening of a mineralization stirrer and be transported to a storage yard or a warehouse.
Carbon dioxide absorption (%) = (mineralized ash after mineralization-unmineralized cement kiln bypass blast ash entering a mineralization mixer-mineralized water weight)/cement kiln bypass blast ash entering a mineralization mixer x 100%, and the absorption of carbon dioxide is detected to be 31%.
Comparative example 1
The stirring water is pure water, and 1 ton of cement kiln bypass blow-off ash is sent into a mineralization stirrer through a cement kiln bypass blow-off ash storage, metering and conveying system; then according to the proportion of 0.2 of water-cement ratio, feeding pure water into a mineralization stirrer through a water supply system, starting the mineralization stirrer to stir for 8 minutes, then introducing 4000Nm 3/h of cement kiln tail waste gas into the mineralization stirrer through a centrifugal fan, mineralizing and stirring for 1.0 hour, detecting the pH value of the material through a pH value online detection system in the mineralization process, slowly adding cement kiln bypass blast ash into the mineralization stirrer, and maintaining the pH value of the material to be between 10 and 11 all the time until mineralization is completed; after mineralization, stopping introducing waste gas at the tail of the cement kiln and stirring, and enabling the generated mineralized ash to enter a mineralized ash conveying system through a discharge opening of a mineralization stirrer and be transported to a storage yard or a warehouse.
Carbon dioxide absorption (%) = (mineralized ash after mineralization-unmineralized cement kiln bypass blast ash entering a mineralization mixer-mineralized water weight)/cement kiln bypass blast ash entering a mineralization mixer x 100%, and the absorption of carbon dioxide is 16%.
Comparative example 2
Adding sodium acetate into a water storage tank through an additive system, controlling the mass fraction of sodium acetate aqueous solution to be 3%, and conveying 1 ton of cement kiln bypass blow-down ash into a mineralization stirrer through a cement kiln bypass blow-down ash storage, metering and conveying system; then, according to the proportion of the water-cement ratio of 0.2, feeding the sodium acetate aqueous solution into a mineralization stirrer through a water supply system, starting the mineralization stirrer to stir for 8 minutes, introducing 4000Nm 3/h cement kiln tail waste gas from a kiln tail chimney into the mineralization stirrer through a centrifugal fan, mineralizing and stirring for 1.0 hour, detecting the pH value of the material through a pH value online detection system in the mineralization process, slowly adding cement kiln bypass vent ash into the mineralization stirrer, and maintaining the pH value of the material to be between 8 and 10 all the time until mineralization is completed; after mineralization, stopping introducing waste gas at the tail of the cement kiln and stirring, and enabling the generated mineralized ash to enter a mineralized ash conveying system through a discharge opening of a mineralization stirrer and be transported to a storage yard or a warehouse.
Carbon dioxide absorption (%) = (mineralized ash after mineralization-unmineralized cement kiln bypass blast ash entering a mineralization mixer-mineralized water weight)/cement kiln bypass blast ash entering a mineralization mixer x 100%, the absorption of carbon dioxide was detected to be 18%.
Comparative example 3
The stirring water is pure water, and 1 ton of cement kiln bypass blow-off ash is sent into a mineralization stirrer through a cement kiln bypass blow-off ash storage, metering and conveying system; then according to the proportion of 0.2 of water-cement ratio, feeding pure water into a mineralization stirrer through a water supply system, starting the mineralization stirrer to stir for 8 minutes, then introducing 4000Nm 3/h of cement kiln tail waste gas into the mineralization stirrer through a centrifugal fan, mineralizing and stirring for 3.0 hours, detecting the pH value of the material through a pH value online detection system in the mineralization process, slowly adding cement kiln bypass blast ash into the mineralization stirrer, and maintaining the pH value of the material to be between 8 and 10 all the time until mineralization is completed; after mineralization, stopping introducing waste gas at the tail of the cement kiln and stirring, and enabling the generated mineralized ash to enter a mineralized ash conveying system through a discharge opening of a mineralization stirrer and be transported to a storage yard or a warehouse.
Carbon dioxide absorption (%) = (mineralized ash after mineralization-unmineralized cement kiln bypass blast ash entering a mineralization mixer-mineralized water weight)/cement kiln bypass blast ash entering a mineralization mixer x 100%, and the absorption of carbon dioxide was measured to be 20%.
Comparative example 4
Adding sodium acetate into a water storage tank through an additive system, controlling the mass fraction of sodium acetate aqueous solution to be 3%, and conveying 1 ton of cement kiln bypass blow-down ash into a mineralization stirrer through a cement kiln bypass blow-down ash storage, metering and conveying system; then, according to the proportion of the water-cement ratio of 0.2, feeding the sodium acetate aqueous solution into a mineralization stirrer through a water supply system, starting the mineralization stirrer to stir for 8 minutes, introducing 4000Nm 3/h cement kiln tail waste gas from a kiln tail chimney into the mineralization stirrer through a centrifugal fan, mineralizing and stirring for 3.0 hours, detecting the pH value of the material through a pH value online detection system in the mineralization process, slowly adding cement kiln bypass vent ash into the mineralization stirrer, and maintaining the pH value of the material to be between 8 and 10 all the time until mineralization is completed; after mineralization, stopping introducing waste gas at the tail of the cement kiln and stirring, and enabling the generated mineralized ash to enter a mineralized ash conveying system through a discharge opening of a mineralization stirrer and be transported to a storage yard or a warehouse.
Carbon dioxide absorption (%) = (mineralized ash after mineralization-unmineralized cement kiln bypass blast ash entering a mineralization mixer-mineralized water weight)/cement kiln bypass blast ash entering a mineralization mixer x 100%, and the absorption of carbon dioxide was detected to be 21%.
Example 1-example 3 show that the system and method provided by the invention have the advantages that the absorption rate of carbon dioxide in kiln tail smoke is more than 30%, the maximum absorption rate is 32%, mineralization can be completed within 0.5-1.5 hours, the mineralization rate is high, and the mineralization degree is high; comparative example 1-comparative example 4 in comparison with example 1, the absorption rate of carbon dioxide could not be improved by prolonging the mineralization time without using sodium acetate or mineralizing pH control range of less than 10 under the same smoke condition.
Finally, it should be noted that: the above embodiments are only for illustrating the technical solution of the present invention, and not for limiting the same; although the 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 scheme described in the foregoing embodiments can be modified or some or all of the technical features thereof can be replaced by equivalents; such modifications and substitutions do not depart from the spirit of the invention.
Claims (7)
1. A method for accelerating CO 2 in mineralized and absorbed smoke by using pH value-controlled calcium carbonate, which is realized by a system for accelerating CO 2 in mineralized and absorbed smoke by using pH value-controlled calcium carbonate, wherein the system comprises a cement kiln bypass blow-off ash storage, metering and conveying system, an additive system, a water supply system, a kiln tail waste gas air supply system, a pH online detection system, a stirring mineralization and absorption system, a decarburization waste gas air-out system and a mineralization ash conveying system;
The outlet of the cement kiln bypass air-release ash storage, metering and conveying system is connected with the feed inlet of the stirring mineralization absorption system, the outlet of the additive system is connected with the inlet of the water supply system, the outlet of the water supply system is connected with the water inlet of the stirring mineralization absorption system, the outlet of the kiln tail waste gas air supply system is connected with the air inlet of the stirring mineralization absorption system, the pH on-line detection system is connected with the pH value sampling port of the stirring mineralization absorption system, the air outlet of the stirring mineralization absorption system is connected with the decarburization waste gas air outlet system, and the discharge port of the stirring mineralization absorption system is connected with the mineralization ash conveying system; the method is characterized in that:
The method comprises the following steps:
s1, adding sodium acetate into a water supply system through an additive system, and controlling the mass fraction of a sodium acetate aqueous solution to be 1-3%;
S2, feeding cement kiln bypass blow-off ash into a stirring mineralization absorption system through a cement kiln bypass blow-off ash storage, metering and conveying system, adding water according to the water-ash ratio of 0.1-0.3, and stirring for a certain time to enable calcium oxide in the cement kiln bypass blow-off ash to be fully hydrated into calcium hydroxide;
S3, diversion of mud kiln tail waste gas from a kiln tail chimney by a kiln tail waste gas air supply system, and feeding into a stirring mineralization absorption system according to the air volume of 3000-5000Nm 3/h, and feeding cement kiln tail waste gas while stirring, mineralizing for 0.5-1.5h, so that CO 2 in the cement kiln tail waste gas is absorbed by cement kiln bypass air release ash to realize permanent solidification;
s4, in the mineralization process, a pH value online detection system is used for monitoring the pH value of the materials in the stirring mineralization absorption system in the whole process, the pH value is ensured to be between 10 and 11, when the pH value is reduced to be less than 10, cement kiln bypass air release ash is slowly added into the stirring mineralization absorption system, and the pH value of the materials is maintained to be between 10 and 11 all the time until mineralization is completed;
S5, after mineralization is completed, stopping introducing waste gas at the tail of the cement kiln, opening a discharge opening of a stirring mineralization absorption system, and transporting the generated mineralized ash to a storage yard or a storage warehouse through a mineralized ash conveying system.
2. The method for accelerating the mineralization and absorption of CO 2 in flue gas by using the pH value regulated and controlled calcium carbonate according to claim 1, wherein the cement kiln bypass blow-down ash storage, metering and conveying system comprises a cement kiln bypass blow-down ash storage bin, an electric gate valve and a screw metering feeder which are connected in sequence, and an outlet of the screw metering feeder is connected with a feed inlet of the stirring mineralization and absorption system.
3. The method for accelerating mineralization and absorption of CO 2 in flue gas by using pH value regulated calcium carbonate according to claim 1, wherein the additive system comprises an additive storage bin, a disk feeder and a feeding chute which are sequentially connected, and an outlet of the feeding chute is connected with an inlet of a water supply system.
4. The method for accelerating mineralization and absorption of CO 2 in flue gas by using pH value regulated calcium carbonate according to claim 1, wherein the water supply system comprises a water storage tank, a metering water pump and a water supply pipeline which are connected in sequence, and an outlet of the water supply pipeline is connected with a water inlet of the stirring mineralization absorption system.
5. The method for accelerating mineralization and absorption of CO 2 in flue gas by using pH value regulated calcium carbonate according to claim 1, wherein the stirring mineralization absorption system comprises a mineralization stirrer, and a feed inlet, a water inlet, a pH value sampling port, an air inlet, an air outlet and a discharge port which are positioned on the mineralization stirrer.
6. The method for accelerating mineralization and absorption of CO 2 in flue gas by using pH value regulated calcium carbonate according to claim 1, wherein the kiln tail waste gas air supply system comprises a centrifugal fan and a kiln tail waste gas air supply pipeline, an inlet of the centrifugal fan is connected with a kiln tail chimney, and an outlet of the centrifugal fan is connected with an air inlet of the stirring mineralization absorption system through the kiln tail waste gas air supply pipeline; the decarburization waste gas air-out system comprises a decarburization waste gas air-out pipeline, an air outlet of the stirring mineralization absorption system is connected with an inlet of the decarburization waste gas air-out pipeline, and an outlet of the decarburization waste gas air-out pipeline is connected with a kiln tail chimney.
7. The method for accelerating the mineralization and absorption of CO 2 in flue gas by using the pH value regulated and controlled calcium carbonate according to claim 1, wherein the pH on-line detection system comprises a sampling device and a detection device, and the sampling device is arranged at a pH value sampling port of a mineralization stirrer.
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