CN109126412B - Method for intensifying mineralization of carbon dioxide by using salt-containing wastewater - Google Patents
Method for intensifying mineralization of carbon dioxide by using salt-containing wastewater Download PDFInfo
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01D53/34—Chemical or biological purification of waste gases
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- 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
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- B—PERFORMING OPERATIONS; TRANSPORTING
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Abstract
The invention discloses a method for strengthening mineralization of carbon dioxide by solid waste by saline wastewater, which comprises a feeding unit, an air inlet unit, a reaction unit and a separation and circulation unit, wherein: the feeding unit comprises a raw material humidifier, a dryer, a first screw feeder and a second screw feeder; the air inlet unit comprises a gas mixer; the reaction unit comprises an air-flow bed reactor and furnace humidifying nozzles arranged at a plurality of positions on the air-flow bed reactor; the separation circulating unit comprises a bag-type dust collector and a draught fan; the method has the advantages that the mineralization efficiency is improved by combining the pretreatment of solid wastes of the mineralization raw materials, the moisture distribution of the salt-containing wastewater of the flue gas and the moisture spraying of the salt-containing wastewater in the reactor, the reaction contact efficiency is improved by adopting the entrained-flow bed reactor, the utilization of the wastes can be effectively improved, the CO2 emission of a power plant can be reduced, and the method is a novel greenhouse gas emission reduction technology which is very suitable for the national conditions of China.
Description
Technical Field
The invention relates to a device and a method for directly trapping carbon dioxide in mineralized flue gas, in particular to a method for strengthening mineralization of carbon dioxide by solid waste by using salt-containing wastewater.
Background
The international energy agency report suggests that CO2 capture and sequestration (CCS) technology is one of three major technologies for effective control of CO2 emissions, providing 19% contribution to the blueprint planned by the united nations 2050 to control global CO2 concentrations at 450ppm, and predicting that 3400 CCS projects will be established worldwide by 2050 to form the 58100 billion dollar CO2 industry. In the last two decades, governments of various countries in the world strive to fund CCS technical research, establish research and development centers and demonstration projects in cooperation with universities and enterprises, and lead the market front to be occupied by the preemptive development of technical patents.
The CO2 mineralization technology is a new research hotspot of the CCS technology in the last decade. The mineralization technology for CO2 removal has the following advantages:
1) the resource reserves are wide, the reserves of mineralized magnesium (calcium) silicate ores (mainly serpentine and olivine) exceed 30000Gt, and the total amount of the resources is more than that of the known fossil energy; industrial massive solid wastes (such as power plant wastes, steel plant residues, cement plant residues and mining plant tailings) can be used as raw materials, so that the win-win situation of waste utilization and environmental protection is realized;
2) the permanent and environment-friendly carbon dioxide sequestration realizes non-leakage and non-later-period monitoring, and compared with geological sequestration, the method reduces the risk and is easily accepted by the public;
3) the carbonation reaction is an exothermic reaction, and theoretically, the requirement on heat can be reduced;
4) the method has good applicability to countries and regions where suitable geological sealing strata cannot be found or pollution sources with high pipeline transportation cost due to too long distance;
5) various products with economic value are generated in the carbonization process, the cost of carbon dioxide treatment can be subsidized, and higher economic benefit can be created with potential to form an industrial chain.
The CO2 mineralization technology has important value for China. China has huge reserves of CO2 mineralized serpentine and olivine, and the total sealed reserve can reach 13000Gt CO2 or so.
The prior device for carbon dioxide mineralization needs to achieve the following goals:
1) reduce the energy consumption required by pretreatment and reaction and develop a new pretreatment device. Such as reducing the temperature and pressure conditions required for the reaction, larger particle size ores are used. Due to the characteristics of ores, different ores are suitable for different pretreatment technologies and need to be treated differently.
2) The reaction speed is accelerated, and the reaction time is shortened. The reaction time of 2-6 hours is reduced to 30-60 min. There is a need to develop chemical reagents with higher ore leaching rates and enhanced carbonation efficiencies.
3) The use of renewable chemical reagents, environmental friendliness and cost reduction are achieved.
Disclosure of Invention
In order to solve the problems in the prior art, the invention provides a method for strengthening mineralization of carbon dioxide by solid wastes through salt-containing wastewater, the mineralization efficiency is improved by a mode of combining pretreatment of solid wastes through mineralization raw materials, moisture distribution of flue gas salt-containing wastewater and moisture spraying of salt-containing wastewater in a reactor, and the reaction contact efficiency is improved by adopting an entrained flow bed reactor.
In order to achieve the purpose, the invention adopts the following technical scheme:
a method for intensifying mineralization of carbon dioxide by solid wastes through saline wastewater adopts a device comprising a feeding unit, an air inlet unit, a reaction unit and a separation and circulation unit, wherein: the feeding unit comprises a raw material bin 1, a dryer 2, a first screw feeder 3 and a second screw feeder 4; the air intake unit includes a gas mixer 5; the reaction unit comprises an air-bed reactor 6 and furnace humidifying nozzles arranged at a plurality of positions on the air-bed reactor 6; the separation circulating unit comprises a bag-type dust collector 10 and an induced draft fan 11;
the specific connection relationship is as follows: an outlet of the raw material bin 1 is connected with an inlet at the upper end of the dryer 2, an outlet at the lower end of the dryer 2 is communicated with an inlet of the first screw feeder 3, and an outlet of the first screw feeder 3 is communicated with a venturi tube inlet at the bottom of the entrained flow reactor 6; the flue gas 12 without CO2 removal is communicated with an inlet at the upper end of a gas mixer 5, an outlet of a water quantitative pump I14 is communicated with an inlet at the lower end of the gas mixer 5, an outlet at the upper end of the gas mixer 5 is communicated with an inlet of an air-flow bed reactor 6, namely a venturi tube at the top, and the humidified flue gas is brought into the air-flow bed reactor 6 for mineralization reaction; the outlet of the water quantitative pump II15 is communicated with a plurality of in-furnace humidifying nozzles arranged on the entrained flow reactor 6, and water is sprayed into the entrained flow reactor 6 to improve the efficiency of removing CO2 by mineralization reaction; an outlet at the lower end of the air flow bed reactor 6 is communicated with an inlet at the right side of the bag-type dust remover 10, a solid outlet at the lower end of the bag-type dust remover 10 is communicated with an inlet of the second screw feeder 4, an outlet of the second screw feeder 4 is communicated with a venturi tube inlet at the bottom of the air flow bed reactor 6, and a solid raw material separated from the bag-type dust remover 10 is returned to the air flow bed reactor 6; and a gas outlet at the upper end of the bag-type dust collector 10 is communicated with an induced draft fan 11, an outlet of the induced draft fan 11 is communicated with the atmosphere, and the flue gas 13 after CO2 is removed is discharged.
The method specifically comprises the following steps:
firstly, raw material pretreatment: the mineralized raw material solid waste is humidified by a raw material bin 1 and then enters a dryer 2 for drying pretreatment;
the second step is that: raw materials enter a reactor: the pretreated mineralized raw material solid waste is conveyed into an air main pipe through a first screw feeder 3 and is carried by air to enter an air-flow bed reactor 6;
step three, flue gas humidity distribution: the salt-containing wastewater for moisture distribution is injected into the gas mixer 5 together with the flue gas 12 without CO2 removal through a water quantitative pump I14, and the moisture distribution amount is adjusted by changing the flow rate of the water quantitative pump I14;
fourthly, the flue gas enters a reactor: the humidified flue gas from the gas mixer 5 enters the entrained-flow bed reactor 6 from a venturi tube at the top of the entrained-flow bed reactor 6;
fifthly, humidifying and mineralizing reaction: secondly, carrying out mineralization reaction on solid waste of the mineralized raw material entering the airflow bed reactor 6 and the flue gas entering the airflow bed reactor 6 in the fourth step to remove CO2 in the flue gas, enabling salt-containing wastewater from a water quantitative pump II15 to enter the airflow bed reactor 6 through furnace humidifying nozzles arranged at multiple positions on the airflow bed reactor 6, enabling the flue gas and the raw material to be subjected to rapid fluidization reaction, and adjusting the moisture distribution capacity in the airflow bed reactor 6 in the mineralization reaction by changing the flow rate of the water quantitative pump II 15;
sixthly, gas-solid separation: after CO2 is removed from the top of the entrained flow reactor 6, the flue gas 13 and the reacted raw materials are cooled, and then enter a bag-type dust collector 10 for gas-solid separation;
step seven, discharging the flue gas: after CO2 is removed after gas-solid separation, the flue gas 13 is led out of the room through a draught fan 11;
eighth, solid returning: the solid raw material after gas-solid separation falls and is collected into a bag-type dust collector 10, and returns to the air-flow bed reactor 6 through a second screw feeder 4 for continuous reaction;
the concentration of carbon dioxide in the flue gas 13 after CO2 is removed by adopting a flue gas analyzer in an on-line analysis manner, and the lower the concentration of the outlet carbon dioxide is, the better the reaction effect is.
The solid waste of the mineralized raw materials is fly ash, carbide slag or steel slag.
The salt-containing wastewater in the third step and the fifth step is underground brine, seawater, salt pan wastewater or industrial wastewater.
And the ratio of the mass of the salt-containing wastewater to the volume of the flue gas in the third step of flue gas humidification is 10-1000 g/Nm & lt 3 & gt.
And the ratio of the mass of the salt-containing wastewater to the volume of the flue gas in the fifth step of humidification and mineralization reaction is 40 g/Nm & lt 3 & gt.
And the mineralization reaction temperature in the fifth step is 450-650 ℃.
The mineralization reaction temperature in the fifth step is 600 ℃.
The ratio of the amount of the mineralized raw material solid waste entering the air flow bed reactor 6 in the second step to the volume of the flue gas entering the air flow bed reactor 6 in the fourth step is 600-1000 g/Nm < 3 >.
Compared with the prior art, the invention has the following beneficial technical effects:
1) the adopted carbon-fixing raw materials are solid wastes, so that the cost is low, the source is wide, and industrial massive solid wastes (coal ash, carbide slag, steel slag and waste cement) can be used as the raw materials, so that the win-win situation of waste utilization and environmental protection is realized;
2) the method for mineralizing carbon dioxide by using the strengthened solid waste containing salt wastewater has wide source on raw materials. The underground brine, the seawater, the salt pan wastewater and the industrial wastewater all contain similar decarburization and carbon sequestration factors, so that the method is favorably suitable for local conditions, and the applicability of the method is improved.
3) Various products with economic value are generated in the carbonization process, the treatment cost of carbon dioxide can be subsidized and captured, and higher economic benefit can be created with potential to form an industrial chain.
Drawings
FIG. 1 is a schematic view of an apparatus for enhancing mineralization of carbon dioxide by solid waste with saline wastewater according to the present invention.
Detailed Description
The invention is described in further detail below with reference to the accompanying drawings.
As shown in fig. 1, the apparatus adopted by the method for enhancing mineralization of carbon dioxide by solid waste by using saline wastewater of the present invention comprises a feeding unit, an air inlet unit, a reaction unit and a separation and circulation unit, wherein: the feeding unit comprises a raw material bin 1, a dryer 2, a first screw feeder 3 and a second screw feeder 4; the air intake unit includes a gas mixer 5; the reaction unit comprises an air-bed reactor 6 and furnace humidifying nozzles arranged at a plurality of positions on the air-bed reactor 6; the separation circulating unit comprises a bag-type dust collector 10 and an induced draft fan 11;
the specific connection relationship is as follows: an outlet of the raw material bin 1 is connected with an inlet at the upper end of the dryer 2, an outlet at the lower end of the dryer 2 is communicated with an inlet of the first screw feeder 3, and an outlet of the first screw feeder 3 is communicated with a venturi tube inlet at the bottom of the entrained flow reactor 6; the flue gas 12 without CO2 removal is communicated with an inlet at the upper end of a gas mixer 5, an outlet of a water quantitative pump I14 is communicated with an inlet at the lower end of the gas mixer 5, an outlet at the upper end of the gas mixer 5 is communicated with an inlet of an air-flow bed reactor 6, namely a venturi tube at the top, and the humidified flue gas is brought into the air-flow bed reactor 6 for mineralization reaction; the outlet of the water quantitative pump II15 is communicated with a plurality of in-furnace humidifying nozzles arranged on the entrained flow reactor 6, and water is sprayed into the entrained flow reactor 6 to improve the efficiency of removing CO2 by mineralization reaction; an outlet at the lower end of the air flow bed reactor 6 is communicated with an inlet at the right side of the bag-type dust remover 10, a solid outlet at the lower end of the bag-type dust remover 10 is communicated with an inlet of the second screw feeder 4, an outlet of the second screw feeder 4 is communicated with a venturi tube inlet at the bottom of the air flow bed reactor 6, and a solid raw material separated from the bag-type dust remover 10 is returned to the air flow bed reactor 6; and a gas outlet at the upper end of the bag-type dust collector 10 is communicated with an induced draft fan 11, an outlet of the induced draft fan 11 is communicated with the atmosphere, and the flue gas 13 after CO2 is removed is discharged.
The invention discloses a method for strengthening mineralization of carbon dioxide by solid wastes by using saline wastewater, which comprises the following steps:
firstly, raw material pretreatment: the mineralized raw material solid waste is humidified by a raw material bin 1 and then enters a dryer 2 for drying pretreatment;
the second step is that: raw materials enter a reactor: the pretreated mineralized raw material solid waste is conveyed into an air main pipe through a first screw feeder 3 and is carried by air to enter an air-flow bed reactor 6;
step three, flue gas humidity distribution: the salt-containing wastewater for moisture distribution is injected into the gas mixer 5 together with the flue gas 12 without CO2 removal through a water quantitative pump I14, and the moisture distribution amount is adjusted by changing the flow rate of the water quantitative pump I14;
fourthly, the flue gas enters a reactor: the humidified flue gas from the gas mixer 5 enters the entrained-flow bed reactor 6 from a venturi tube at the top of the entrained-flow bed reactor 6;
fifthly, humidifying and mineralizing reaction: secondly, carrying out mineralization reaction on solid waste of the mineralized raw material entering the airflow bed reactor 6 and the flue gas entering the airflow bed reactor 6 in the fourth step to remove CO2 in the flue gas, enabling salt-containing wastewater from a water quantitative pump II15 to enter the airflow bed reactor 6 through furnace humidifying nozzles arranged at multiple positions on the airflow bed reactor 6, enabling the flue gas and the raw material to be subjected to rapid fluidization reaction, and adjusting the moisture distribution capacity in the airflow bed reactor 6 in the mineralization reaction by changing the flow rate of the water quantitative pump II 15;
sixthly, gas-solid separation: after CO2 is removed from the top of the entrained flow reactor 6, the flue gas 13 and the reacted raw materials are cooled, and then enter a bag-type dust collector 10 for gas-solid separation;
step seven, discharging the flue gas: after CO2 is removed after gas-solid separation, the flue gas 13 is led out of the room through a draught fan 11;
eighth, solid returning: the solid raw material after gas-solid separation falls and is collected into a bag-type dust collector 10, and returns to the air-flow bed reactor 6 through a second screw feeder 4 for continuous reaction;
the concentration of carbon dioxide in the flue gas 13 after CO2 is removed by adopting a flue gas analyzer in an on-line analysis manner, and the lower the concentration of the outlet carbon dioxide is, the better the reaction effect is.
In a preferred embodiment of the present invention, the solid waste of the mineralized raw material is fly ash, carbide slag or steel slag.
In a preferred embodiment of the present invention, the salt-containing wastewater in the third and fifth steps is underground brine, seawater, salt pan wastewater or industrial wastewater.
In a preferred embodiment of the invention, the ratio of the mass of the salt-containing wastewater to the volume of the flue gas in the third step of flue gas humidification is 10-1000 g/Nm 3.
As a preferred embodiment of the invention, the ratio of the mass of the salt-containing wastewater to the volume of the flue gas in the fifth humidification and mineralization reaction step is 10-100 g/Nm 3, and more preferably 40 g/Nm 3.
As a preferred embodiment of the invention, the temperature of the mineralization reaction in the fifth step is 450-650 ℃, more preferably 600 ℃.
In a preferred embodiment of the present invention, the ratio of the amount of the solid waste of the mineralized raw material entering the entrained flow reactor 6 in the second step to the volume of the flue gas entering the entrained flow reactor 6 in the fourth step is 600 to 1000g/Nm 3.
The specific embodiment is as follows:
example 1
The simulated flue gas containing 15% of carbon dioxide by volume and the balance of nitrogen is adopted for reaction, and one of fly ash, carbide slag, steel slag and waste cement is respectively adopted as a raw material. The method is characterized in that salt-containing wastewater is not added for reinforcement, the mineralization reaction temperature is 600 ℃, and the solid waste feeding amount is 750 g/Nm & lt 3 & gt (flue gas); the carbon dioxide concentration in the inlet flue gas is 15%, and the experimental result in table 1 shows that the effect is the best when the fly ash is adopted, and the outlet carbon dioxide concentration is 13%.
TABLE 1 concentration of carbon dioxide at the outlet of flue gas after mineralization of different mineralized raw materials
| Mineralizing a feedstock | Fly ash | Carbide slag | Steel slag | Waste cement |
| Outlet carbon dioxide concentration (%) | 13 | 14 | 12 | 14 |
Example 2
The fly ash in the solid waste is used as a raw material, one of underground brine, seawater, salt pan wastewater and industrial wastewater is respectively injected into a gas mixer 5 together with the pre-decarburization flue gas through a water quantitative pump I14, and the moisture distribution capacity of the flue gas is 400g (salt-containing wastewater)/Nm 3 (flue gas); the water spray capacity in the entrained flow reactor was 40g (saline wastewater)/Nm 3 (flue gas). The other conditions were the same as in example 1, and the results in Table 2 show that the effect was the best when using the underground brine, and the outlet carbon dioxide concentration was 8%.
TABLE 2 concentration of carbon dioxide at the exit of flue gas after mineralization of different strengthening components
| Fortifying component | Brine | Seawater, its production and use | Salt pan wastewater | Industrial waste water |
| Outlet carbon dioxide concentration (%) | 8 | 12 | 10 | 11 |
Example 3
Coal ash in solid waste is used as a raw material, underground brine is used for reinforcement, and the moisture content of flue gas is 100g (underground brine)/Nm 3 (flue gas), 300g (underground brine) Nm 3 (flue gas), 400g (underground brine)/Nm 3 (flue gas), 500g (underground brine)/Nm 3 (flue gas), 600g (underground brine)/Nm 3 (flue gas), 800g (underground brine)/Nm 3 (flue gas) and 1000g (underground brine)/Nm 3 (flue gas); the same conditions as in example 2 are applied to the conditions of the moisture content in the entrained flow reactor being 0g (underground brine)/Nm 3, and the experimental results in table 3 show that the effect of the moisture content in the flue gas being 400 g/Nm 3 (flue gas) is the best, and then the outlet concentration of the carbon dioxide is increased to be 11% without changing the outlet concentration of the carbon dioxide with the moisture content in the flue gas, so that the moisture content in the flue gas is selected to be 400g (underground brine)/Nm 3 (flue gas).
TABLE 3 concentration of carbon dioxide at the outlet of flue gas after mineralization reaction with different raw material moisture distribution
| Raw material moisture content (g/Nm 3) | 100 | 300 | 400 | 500 | 600 | 800 | 1000 |
| Outlet carbon dioxide concentration (%) | 13 | 13 | 11 | 11 | 11 | 11 | 11 |
Example 4
Coal ash in solid waste is used as a raw material, underground brine is used for reinforcement, and the water spraying amount in the entrained flow reactor is 10g (underground brine)/Nm 3 (flue gas), 30g (underground brine)/Nm 3 (flue gas), 40g (underground brine)/Nm 3 (flue gas), 50g (underground brine)/Nm 3 (flue gas), 60g (underground brine)/Nm 3 (flue gas), 80g (underground brine)/Nm 3 (flue gas) and 10g (underground brine)/Nm 3 (flue gas); other conditions are the same as example 2, and the experimental results in table 4 show that the effect is the best when the moisture content in the entrained flow reactor is 40g (underground brine)/Nm 3 (flue gas), and then the outlet concentration of carbon dioxide with the moisture content is continuously increased and is unchanged, and the outlet concentration of carbon dioxide is 8%, so that the moisture content in the entrained flow reactor is 40g (underground brine)/Nm 3 (flue gas).
TABLE 4 concentration of carbon dioxide at the flue gas outlet after mineralization reaction at the moisture injection rates in the different reactors
| Raw material moisture content (g/Nm 3) | 10 | 30 | 40 | 50 | 60 | 80 | 100 |
| Outlet carbon dioxide concentration (%) | 11 | 10 | 8 | 8 | 8 | 8 | 8 |
Example 5
Coal ash in solid waste is used as a raw material, underground brine is used for reinforcement, and the mineralization reaction temperature is 450 ℃, 500 ℃, 550 ℃, 600 ℃ and 650 ℃; the other conditions are the same as example 2, and the results in Table 5 show that the mineralization reaction temperature is 600 ℃ which is the best, the outlet carbon dioxide concentration is not changed when the temperature is continuously raised, and the outlet carbon dioxide concentration is 8%, so the reaction temperature is 600 ℃.
TABLE 5 concentration of carbon dioxide at the flue gas outlet after mineralization reactions at different mineralization reaction temperatures
| Reaction temperature (. degree.C.) | 450 | 500 | 550 | 600 | 650 |
| Outlet carbon dioxide concentration (%) | 11 | 10 | 9 | 8 | 8 |
Example 6
The method is characterized in that fly ash in solid waste is used as a raw material, underground brine is used for reinforcement, and the feeding amount of the fly ash in the solid waste is 600 g/Nm & lt 3 & gt (flue gas), 700 g/Nm & lt 3 & gt (flue gas), 750 g/Nm & lt 3 & gt (flue gas), 800 g/Nm & lt 3 & gt (flue gas), 900 g/Nm & lt 3 & gt (flue gas) and 1000g/Nm & lt 3 & gt (flue gas); under the same other conditions as in example 2, it is understood from the results of the experiment in Table 6 that the effect is the best when the solid waste is fed in an amount of 750 g/Nm 3 (flue gas), and the solid waste is fed in an amount of 750 g/Nm 3 (flue gas) because the outlet carbon dioxide concentration is 8% and the outlet carbon dioxide concentration is unchanged by continuously increasing the feed amount.
TABLE 6 carbon dioxide concentration at the flue gas outlet after mineralization reactions at different solid feed rates
| Amount of solid feed (g (aqueous solution)/Nm 3) | 600 | 700 | 750 | 800 | 900 | 1000 |
| Outlet carbon dioxide concentration (%) | 11 | 9 | 8 | 8 | 8 | 8 |
Claims (3)
1. A method for strengthening mineralization of carbon dioxide by saline wastewater is characterized in that: the device adopted by the method comprises a feeding unit, a gas inlet unit, a reaction unit and a separation and circulation unit, wherein: the feeding unit comprises a raw material bin (1), a dryer (2), a first screw feeder (3) and a second screw feeder (4); the air intake unit comprises a gas mixer (5); the reaction unit comprises an air-flow bed reactor (6) and in-furnace humidifying nozzles arranged at a plurality of positions on the air-flow bed reactor (6); the separation circulating unit comprises a bag-type dust collector (10) and an induced draft fan (11);
the specific connection relationship is as follows: an outlet of the raw material bin (1) is connected with an inlet at the upper end of the dryer (2), an outlet at the lower end of the dryer (2) is communicated with an inlet of the first screw feeder (3), and an outlet of the first screw feeder (3) is communicated with a Venturi tube inlet at the bottom of the entrained flow reactor (6); the flue gas (12) without CO2 removal is communicated with an inlet at the upper end of a gas mixer (5), an outlet of a water quantitative pump I (14) is communicated with an inlet at the lower end of the gas mixer (5), an outlet at the upper end of the gas mixer (5) is communicated with an inlet of an air-flow bed reactor (6), namely a venturi tube at the top, and the humidified flue gas is brought into the air-flow bed reactor (6) for mineralization reaction; the outlet of the water quantitative pump II (15) is communicated with furnace humidifying nozzles arranged at a plurality of positions on the air-flow bed reactor (6), and water is sprayed into the air-flow bed reactor (6) to improve the efficiency of removing CO2 by mineralization reaction; an outlet at the lower end of the air flow bed reactor (6) is communicated with an inlet at the right side of the bag-type dust collector (10), a solid outlet at the lower end of the bag-type dust collector (10) is communicated with an inlet of the second screw feeder (4), an outlet of the second screw feeder (4) is communicated with a Venturi tube inlet at the bottom of the air flow bed reactor (6), and a solid raw material obtained by separating from the bag-type dust collector (10) is returned to the air flow bed reactor (6); a gas outlet at the upper end of the bag-type dust collector (10) is communicated with an induced draft fan (11), an outlet of the induced draft fan (11) is communicated with the atmosphere, and the flue gas (13) after CO2 is removed is discharged;
the method specifically comprises the following steps:
firstly, raw material pretreatment: the mineralized raw material solid waste is humidified by a raw material bin (1) and then enters a dryer (2) for drying pretreatment;
the second step is that: raw materials enter a reactor: the pretreated mineralized raw material solid waste is conveyed into an air main pipe through a first screw feeder (3) and is carried into an air-flow bed reactor (6) by air;
step three, flue gas humidity distribution: the salt-containing wastewater for moisture distribution is injected into a gas mixer (5) together with the flue gas (12) without CO2 removal through a water quantitative pump I (14), and the moisture distribution amount is adjusted by changing the flow rate of the water quantitative pump I (14);
fourthly, the flue gas enters a reactor: the humidified flue gas from the gas mixer (5) enters the entrained-flow bed reactor (6) from a Venturi tube at the top of the entrained-flow bed reactor (6);
fifthly, humidifying and mineralizing reaction: secondly, carrying out mineralization reaction on mineralized raw material solid waste entering the air flow bed reactor (6) and the flue gas entering the air flow bed reactor (6) in the fourth step to remove CO2 in the flue gas, enabling salt-containing wastewater coming out of a water quantitative pump II (15) to enter the air flow bed reactor (6) through furnace humidifying nozzles arranged at multiple positions on the air flow bed reactor (6) to enable the flue gas and the raw materials to be subjected to rapid fluidization reaction, and adjusting the moisture distribution capacity in the air flow bed reactor (6) in the mineralization reaction by changing the flow of the water quantitative pump II (15);
sixthly, gas-solid separation: after CO2 is removed from the top of the entrained flow reactor (6), the flue gas (13) and the reacted raw materials are cooled, and then the flue gas and the reacted raw materials enter a bag-type dust collector (10) for gas-solid separation;
step seven, discharging the flue gas: after CO2 is removed after gas-solid separation, the flue gas (13) is led out of the room through a draught fan (11);
eighth, solid returning: the solid raw material after gas-solid separation falls and is collected in a bag-type dust collector (10), and returns to the air-flow bed reactor (6) for continuous reaction through a second screw feeder (4);
the concentration of carbon dioxide in the flue gas (13) after CO2 is removed is analyzed on line by using a flue gas analyzer, and the lower the concentration of the outlet carbon dioxide is, the better the reaction effect is;
the salt-containing wastewater in the third step and the fifth step is underground brine, seawater, salt pan wastewater or industrial wastewater;
the ratio of the mass of the salt-containing wastewater to the volume of the flue gas in the third step of flue gas humidification is 10-1000 g/Nm 3;
the ratio of the mass of the salt-containing wastewater to the volume of the flue gas in the humidification and mineralization reaction in the fifth step is 40 g/Nm & lt 3 & gt; the mineralization reaction temperature of the fifth step is 450-650 ℃;
the ratio of the amount of the mineralized raw material solid waste entering the air flow bed reactor (6) in the second step to the volume of the flue gas entering the air flow bed reactor (6) in the fourth step is 600-1000 g/Nm & lt 3 & gt.
2. The method for enhancing mineralization of carbon dioxide by saline wastewater as claimed in claim 1, wherein said method comprises the steps of: the solid waste of the mineralized raw materials is fly ash, carbide slag or steel slag.
3. The method for enhancing mineralization of carbon dioxide by saline wastewater as claimed in claim 1, wherein said method comprises the steps of: the mineralization reaction temperature in the fifth step is 600 ℃.
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| CN111085101B (en) * | 2019-12-25 | 2021-03-09 | 华北电力大学 | System and method for mineralizing, sealing and solidifying heavy metals in fly ash by using carbon dioxide |
| CN113025832B (en) * | 2021-03-02 | 2022-07-15 | 重庆大学 | Nickel extraction and CO mineralization from laterite-nickel ore2Method (2) |
| CN115025592A (en) * | 2022-04-01 | 2022-09-09 | 江西理工大学 | Copper tailings adsorbing CO 2 Device for measuring the position of a moving object |
| CN115228414A (en) * | 2022-07-14 | 2022-10-25 | 武汉科技大学 | CO (carbon monoxide) for mineralizing and storing vanadium tailings 2 Reactor (a) |
| CN116492828A (en) * | 2023-04-18 | 2023-07-28 | 湖南工业大学 | Device for mineralizing and sealing carbon dioxide by using fly ash |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1515349A (en) * | 2003-08-25 | 2004-07-28 | 武汉凯迪电力股份有限公司 | Dry flue gas desulfurizing process with independent feeding, back-returning and water-spraying devices |
| US20090255444A1 (en) * | 2008-04-11 | 2009-10-15 | Enrique Ramon Martinez Vera | Method for capturing co2 produced by cement plants by using the calcium cycle |
| US20110206586A1 (en) * | 2010-02-25 | 2011-08-25 | Nol-Tec Systems, Inc. | Fluidized Bed Carbon Dioxide Scrubber For Pneumatic Conveying System |
| CN103566725A (en) * | 2013-10-15 | 2014-02-12 | 中国科学院过程工程研究所 | Device and method for jointly removing sulphur, saltpeter and mercury by semidry method through circulating fluidized bed |
| CN203447967U (en) * | 2013-08-05 | 2014-02-26 | 河北环科力创环境工程有限公司 | Combined smoke desulfuration, denitration and demercuration device of industrial boiler |
| CN104759203A (en) * | 2015-03-17 | 2015-07-08 | 华能国际电力股份有限公司 | Fluidized bed technology and fluidized bed system for directly capturing CO2 in mineralized flue gas |
| CN206064142U (en) * | 2016-08-05 | 2017-04-05 | 南京中电环保科技有限公司 | A kind of spouted fluidized bed desulfuring and denitrifying apparatus |
| CN108310960A (en) * | 2018-03-06 | 2018-07-24 | 浙江哲丰能源发展有限公司 | A kind of method of desulphurization in circulating fluidized bed boiler |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| BRPI0915192A2 (en) * | 2008-06-17 | 2019-04-16 | Calera Corp | methods and systems for using metal oxide waste sources |
-
2018
- 2018-08-20 CN CN201810948855.5A patent/CN109126412B/en active Active
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1515349A (en) * | 2003-08-25 | 2004-07-28 | 武汉凯迪电力股份有限公司 | Dry flue gas desulfurizing process with independent feeding, back-returning and water-spraying devices |
| US20090255444A1 (en) * | 2008-04-11 | 2009-10-15 | Enrique Ramon Martinez Vera | Method for capturing co2 produced by cement plants by using the calcium cycle |
| US20110206586A1 (en) * | 2010-02-25 | 2011-08-25 | Nol-Tec Systems, Inc. | Fluidized Bed Carbon Dioxide Scrubber For Pneumatic Conveying System |
| CN203447967U (en) * | 2013-08-05 | 2014-02-26 | 河北环科力创环境工程有限公司 | Combined smoke desulfuration, denitration and demercuration device of industrial boiler |
| CN103566725A (en) * | 2013-10-15 | 2014-02-12 | 中国科学院过程工程研究所 | Device and method for jointly removing sulphur, saltpeter and mercury by semidry method through circulating fluidized bed |
| CN104759203A (en) * | 2015-03-17 | 2015-07-08 | 华能国际电力股份有限公司 | Fluidized bed technology and fluidized bed system for directly capturing CO2 in mineralized flue gas |
| CN206064142U (en) * | 2016-08-05 | 2017-04-05 | 南京中电环保科技有限公司 | A kind of spouted fluidized bed desulfuring and denitrifying apparatus |
| CN108310960A (en) * | 2018-03-06 | 2018-07-24 | 浙江哲丰能源发展有限公司 | A kind of method of desulphurization in circulating fluidized bed boiler |
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