CN115945054B - CO (carbon monoxide) 2 Method for absorbing and desorbing solid waste resource utilization - Google Patents
CO (carbon monoxide) 2 Method for absorbing and desorbing solid waste resource utilization Download PDFInfo
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- CN115945054B CN115945054B CN202310245241.1A CN202310245241A CN115945054B CN 115945054 B CN115945054 B CN 115945054B CN 202310245241 A CN202310245241 A CN 202310245241A CN 115945054 B CN115945054 B CN 115945054B
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Abstract
The application relates to a CO 2 Method for absorbing and desorbing solid waste resource utilization and relates to CO 2 The technical field of treatment. The method comprises the following steps of 2 The mixed waste gas is injected into the gas-liquid cross-flow hypergravity reactor from the lower part, and the amine absorbent solution at the upper part of the gas-liquid cross-flow hypergravity reactor is utilized to absorb CO 2 The mixed waste gas is trapped, sheared and reacted to obtain the CO-containing catalyst 2 Amine absorption liquid of (2); will contain CO 2 Pumping the amine absorption liquid and solid waste slurry into an impinging stream supergravity reactor from the upper part, obtaining mixed liquid through collision, mixing and reaction, discharging and separating the mixed liquid to realize CO 2 The absorption and desorption have the resource utilization of solid waste. The method realizes CO 2 The mixed waste gas contacts with amine absorbent solution in the cross flow in the high-speed rotating gas-liquid cross flow hypergravity reactor, and 90% -98% of CO can be obtained 2 And (5) absorption and trapping. Captured CO 2 The mixed waste gas can be discharged or desulfurized and denitrated according to the situation.
Description
Technical Field
The present application relates to CO 2 The technical field of treatment, in particular to a CO 2 The absorption and desorption method has the resource utilization of solid waste.
Background
With the development of human society, a great deal of substance energy is consumed, and a great deal of CO is produced 2 Causing global climate problems to change dramatically. CO after combustion at present 2 The capture technology is one of the most commonly used CO 2 Emission reduction technology, and CO after combustion 2 The trapping technology is to separate and recycle CO in the flue gas by using various technical means after the fuel is combusted 2 According to the separation method, the CO after combustion 2 The trapping technique can be divided into: chemical absorption method, solid adsorption method, membrane separation method, temperature-based phase separation method, etc., and the chemical absorption method is to use CO 2 And chemistryChemical reaction between the absorbents will CO 2 Technology for selectively separating gases from flue gases, which is a continuous cyclic process comprising CO 2 Absorption and desorption. In the process, the absorbent selectively absorbs CO in the flue gas at a lower temperature in the absorption tower 2 CO formation 2 Rich liquid. CO then 2 The rich liquid releases the absorbed CO at a higher temperature in the resolving tower 2 And to achieve absorbent regeneration. The process can efficiently remove CO from flue gas 2 And producing high purity CO 2 CO in flue gas 2 The removal efficiency of (3) can reach 99%, nevertheless, the process still faces the great challenges of high energy consumption and high investment operation costs.
Membrane separation technology for CO 2 There is a high cost of separation and its stability and selectivity are to be further optimized. CO using solid materials 2 Trapping has many advantages such as less byproducts generated during recycling, ease of disposal of waste solid adsorbent, etc. However, there are low adsorption amount, low adsorption efficiency, and the like.
In addition, with the rapid development of industrial society, some solid wastes rich in metal oxide components such as calcium and magnesium are very harmful to the environment and difficult to treat, the solid wastes are generally alkaline, the leaching of heavy metal ions in the components of the solid wastes can cause very great pollution to land and underground water resources, among the solid wastes, including steel-making waste residues, fly ash of coal-fired power plants, fly ash left after garbage incineration, shale fly ash, carbide slag, waste building materials and tailings such as serpentine tailings and the like in certain metal smelting processes, the solid wastes are rich in metal elements, can provide a large amount of calcium and magnesium metal oxide, such as CaO/MgO in the steel-making solid waste residues accounts for about 30% -60% of the total mass percentage, caO in the coal-fired power plants exists about 65% of the mass percentage of CaO, caO in the fly ash left after municipal solid waste incineration is about 30% of the like, and many of the wastes are obtained after high-temperature processes, have high reactivity and are used for CO through carbonation reaction 2 Not only can reduce in the emission reduction processThe pollution of solid waste to the environment can fix CO at the same time 2 。
At present in CO 2 In the treatment technology, CO 2 Is the technical key point of the capture and the sealing of the (C) and relates to the CO 2 Effect of emission control. Among the above trapping technologies, the chemical absorption method is the trapping technology with the highest trapping efficiency and the best applicability, but the relatively pure CO obtained after trapping and purification 2 How to fix the chemical absorbent safely for a long time to separate the chemical absorbent from the atmosphere, thereby achieving the purpose of relieving the greenhouse effect, reducing the consumption of the chemical absorbent, improving the recycling rate of the chemical absorbent and becoming the current CO 2 Emission reduction technology focuses on the problem.
Disclosure of Invention
Therefore, the application aims to solve the technical problems of CO trapping by a chemical absorption method in the prior art 2 The chemical absorbent can not be recycled and has large dosage, and simultaneously solves the problems that the solid waste directly fixes CO 2 Low fixation rate, low efficiency and slow reaction.
In order to solve the technical problems, the application provides a CO 2 The method for absorbing and desorbing and recycling the solid waste comprises the following two processes: firstly, absorbing CO in a first gas-liquid cross-flow hypergravity reactor by adopting an amine absorbent 2 Chemical regeneration is achieved by precipitation reactions (pH changes); then contains CO 2 The amine absorption liquid enters an impinging stream supergravity reactor to react with solid waste slurry, and the acid-base neutralization reaction principle is utilized to carry out CO 2 By CaCO 3 And MgCO 3 Is fixed.
The application aims to provide a CO 2 The method for absorbing and desorbing and recycling the solid waste takes a recycling system as a generating device, wherein the recycling system comprises a gas-liquid cross-flow hypergravity reactor and an impinging stream hypergravity reactor, and the gas-liquid cross-flow hypergravity reactor is used for recycling CO 2 The mixed waste gas is quickly transferred into amine absorbent solution, and the impinging stream supergravity reactor is used for converting CO-containing gas 2 Amine absorption liquid and solid waste of (a)Fully contacting the waste slurry; the method comprises the following steps:
(1) CO is processed by 2 Injecting mixed waste gas into the gas-liquid cross-flow hypergravity reactor from the lower part, and utilizing amine absorbent solution at the upper part of the gas-liquid cross-flow hypergravity reactor to perform CO 2 The mixed waste gas is trapped, sheared and reacted to obtain the CO-containing catalyst 2 Amine absorption liquid of (2); the amine absorbent in the amine absorbent solution is diethanolamine and/or N-methyldiethanolamine;
(2) The CO-containing component in the step (1) 2 Pumping the amine absorption liquid and solid waste slurry into the impinging stream hypergravity reactor from the upper part, and obtaining mixed liquid through collision, mixing and reaction, wherein the mixed liquid is discharged and separated to realize CO 2 The absorption and desorption have the resource utilization of solid waste; the solid waste in the solid waste slurry is one or more of carbide slag, shale fly ash and steel slag.
In one embodiment of the application, the hypergravity factors of the gas-liquid cross-flow hypergravity reactor and the impinging stream hypergravity reactor are both 80-120.
In one embodiment of the present application, in step (1), the CO 2 The mixed exhaust gas includes flue gas.
In one embodiment of the present application, in step (1), the CO 2 The components of the mixed waste gas comprise carbon dioxide, nitrogen and sulfur dioxide; the volume ratio of the carbon dioxide to the nitrogen to the sulfur dioxide is 15:79.9:0.1.
in one embodiment of the present application, in step (1), the CO 2 The gas flow rate of the mixed waste gas is 50m 3 /h-150m 3 /h。
In one embodiment of the application, in step (1), the mass concentration of the amine absorbent solution is 30% -50%; the amine absorbent solution is at a temperature of 40 ℃ to 50 ℃ which is also closer to the flue gas temperature.
In one embodiment of the present application, in the step (2), the solid waste is a solid rich in metal oxide components such as calcium and magnesiumThe waste has high content of calcium, high reactivity, and can be used as CO 2 Fixed raw material with higher CO 2 The sealing potential, and the final product obtained after sealing can be harmlessly treated and recycled in roadbed or other building materials, thereby realizing energy conservation, emission reduction and comprehensive utilization of solid waste resources.
In one embodiment of the present application, in step (2), the solid waste slurry has a liquid-to-solid ratio of 10 to 20:1 (L/Kg). Calcium ion (Ca) in the slurry 2+ ) And magnesium ion (Mg) 2+ ) The free movement of (2) increases the chance of ion-ion contact with each other, thereby increasing the reaction rate. When the solid waste is added into deionized water, hydration reaction can firstly occur to convert CaO and MgO into Ca (OH) 2 、Mg(OH) 2 The method comprises the steps of carrying out a first treatment on the surface of the Then Ca (OH) 2 、Mg(OH) 2 Dissolving the obtained Ca 2+ 、Mg 2+ And OH (OH) - Diffuse into the solution, the solution becomes strongly alkaline and Ca 2+ 、Mg 2+ Is in a supersaturated state.
In one embodiment of the present application, in step (2), the CO-containing gas is 2 The liquid flow rate of the amine absorption liquid is 1.5m 3 /h-1.8m 3 /h。
In one embodiment of the present application, in step (2), the liquid flow rate of the solid waste slurry is 1.5m 3 /h-1.8m 3 /h。
Compared with the prior art, the technical scheme of the application has the following advantages:
(1) The method for recycling the CO realizes the CO 2 The mixed waste gas contacts with amine absorbent in the cross flow in the high-speed rotating gas-liquid cross flow hypergravity reactor, and 90% -98% of CO can be obtained 2 And (5) absorption and trapping. Captured CO 2 The mixed waste gas can be discharged or desulfurized and denitrated according to the situation. In the process, the micro-nano scale liquid drop, liquid wire or liquid film formed by the amine absorbent has extremely large phase area, and the surfaces are updated quickly under the action of supergravity, thereby greatly strengthening the transmission rate between gas and liquid and improving CO 2 Absorption trapping efficiency.
(2) The method for recycling utilizes the gas-liquid cross-flow hypergravity reactor to strengthen CO 2 And the process of quickly transferring the mixed waste gas from the gas phase to the liquid phase obviously improves the absorption rate and the purification effect. The high dispersion of the amine absorbent by the supergravity can reduce the consumption of the absorbent, reduce the gas phase resistance passing through the equipment and save the power consumption of a pump and a fan.
(3) The method for recycling utilizes the filler in the impinging stream supergravity reactor to shear the liquid into a micro-nano liquid form, strengthens the update rate of the liquid surface, increases the turbulence of the liquid and promotes the separation of boundary layers, thereby remarkably strengthening the liquid-liquid contact process and improving the precipitation reaction efficiency.
Drawings
In order that the application may be more readily understood, a more particular description of the application will be rendered by reference to specific embodiments thereof that are illustrated in the appended drawings.
FIG. 1 is a CO of the present application 2 The absorption and desorption process flow chart has the resource utilization of the solid waste.
FIG. 2 is a schematic diagram of a gas-liquid cross-flow supergravity reactor of the present application.
FIG. 3 is a schematic diagram of a liquid distributor in a gas-liquid cross-flow supergravity reactor according to the present application.
FIG. 4 is a schematic of an impinging stream supergravity reactor of the present application.
FIG. 5 is the result of thermogravimetric analysis of the solid product of test example 1 of the present application.
FIG. 6 is a graph of gas flow versus CO for test example 2 of the present application 2 Graph of the influence of absorption.
FIG. 7 is a graph of amine absorbent concentration versus CO for test example 3 of the present application 2 Graph of the influence of absorption.
FIG. 8 is a graph showing the hypergravity factor versus CO for test example 4 of the present application 2 Graph of the influence of absorption.
FIG. 9 is a graph showing the cyclic regeneration of the amine absorbent of test example 5 of the present application.
Description of the specification reference numerals: 100-gas-liquid cross flow supergravity reactor, 101-first rotating shaft, 102-liquid distributor, 1021-water outlet, 103-first rotating joint, 104-airtight, 105-first rotating body, 106-gas outlet, 107-first wire mesh, 108-first shell, 109-first shaft seal, 110-first liquid outlet, 200-impinging stream supergravity reactor, 201-second rotating shaft, 202-second rotating joint, 203-second rotating body, 204-second wire mesh, 205-first liquid nozzle, 206-second liquid nozzle, 207-first liquid pipeline, 208-second liquid pipeline, 209-second shell, 210-second liquid outlet, 211-second shaft seal.
Detailed Description
The present application will be further described with reference to the accompanying drawings and specific examples, which are not intended to be limiting, so that those skilled in the art will better understand the application and practice it.
In the present application, unless otherwise indicated, CO 2 The absorptivity calculation formula is:CO 2 absorption rate = (C in V in -C out V out )/C in V in The method comprises the steps of carrying out a first treatment on the surface of the Wherein, the liquid crystal display device comprises a liquid crystal display device,C in 、C out for import and export of CO to reaction system 2 Volume concentration (%),V in 、V out for inlet and outlet gas flow (m) 3 /h）。
In the present application, unless otherwise specified, the hypergravity factor calculation formula is:the method comprises the steps of carrying out a first treatment on the surface of the Wherein, the rotation speed of the n-rotor is r/min; radius of r-rotor, m;
in the present application, unless otherwise indicated, CO 2 The method for absorbing and desorbing and recycling the solid waste mainly comprises five modules, wherein a recycling system is used as a generating device as shown in fig. 1: flue gas simulation gas distribution part, gas-liquid cross flow hypergravity reactor, impinging stream hypergravity reactor, liquid storage solid-liquid separation part and flue gas analysisAnd a detection section. The smoke simulation gas distribution part consists of a plurality of gas bottles, an air compressor, a gas buffer tank, a gas flowmeter, a two-way valve and a three-way valve.
In the present application, unless otherwise specified, the gas-liquid cross-flow hypergravity reactor 100 is connected to a gas buffer tank of a flue gas simulation gas distribution part, and the specific structure is as shown in fig. 2-3: it comprises a liquid distributor 102, a first rotation body 105 and a first housing 108, the first housing 108 being provided with a gas outlet 106 and a first liquid outlet 110; the liquid distributor 102 is disposed through the first housing 108, introducing and spraying liquid; the first rotary body 105 has a first wire mesh 107 and the first rotary body 105 is disposed within a first housing 108; the hermetic seal 104, the hermetic seal 104 is a sealing device that seals the gap of the rotating shaft by compressed air and does not leak the working medium;
the liquid distributor 102 comprises a central tube, and a plurality of water outlets 1021 are formed along the length direction of the central tube; the end part of the central tube is connected with a first rotating shaft 101, and the first rotating shaft 101 is connected with a first driving source through a first rotary joint 103;
the two ends of the first rotating shaft 101 are provided with first rotating joints 103, wherein one first rotating joint 103 is a gas inlet, and the other first rotating joint 103 is a liquid inlet. A first shaft seal 109 is arranged at the joint of one end of the first rotating shaft 101 and the first shell 108, and the first shaft seal 109 is a sealing ring, namely, one end of the first rotating shaft 101 is sealed in a sealing ring mode;
the first rotating body 105 includes a first upper rotating disc and a first lower rotating disc, on which the first wire mesh 107 is disposed; the first upper rotating disk and the first lower rotating disk are respectively provided with a first channel for penetrating the liquid distributor 102. The first wire mesh 107 is a filler, and the filler is an annular disc-shaped filler formed by winding and overlapping a plurality of parallel corrugated wire meshes.
In the present application, unless otherwise specified, the impinging stream supergravity reactor 200 is connected with the aeration liquid cross flow supergravity reactor 100, and the specific structure is shown in fig. 4; which comprises a second rotator 203, a first liquid line 207, a second liquid line 208 and a second housing 209, the second housing 209 being provided with a second liquid outlet 210; the second rotary body 203 has a second wire net 204 and the second rotary body 203 is disposed in a second housing 209, a first liquid line 207 communicates with the first liquid outlet 110, and a second liquid line 208 introduces and sprays liquid;
the second rotating body 203 includes a second upper rotating disk and a second lower rotating disk, on which the second wire mesh 204 is disposed; the second upper rotating disk and the second lower rotating disk are provided with a second channel for penetrating the first liquid pipeline 207 and the second liquid pipeline 208; the second rotating body 203 is connected to the second rotating shaft 201, and the second rotating shaft 201 is connected to the second driving source. Wherein the second wire mesh 204 is a filler, and the filler is an annular disc-shaped filler formed by winding and overlapping a plurality of parallel corrugated wire meshes;
one end of the second rotating shaft 201 is provided with a second rotating joint 202, and the second rotating joint 202 is used for connecting with a driving source such as an output end of a commercial motor. A second shaft seal 211 is arranged at the joint of one end of the second rotating shaft 201 and the second housing 209, and the second shaft seal 211 is a sealing ring, namely, one end of the second rotating shaft 201 is sealed in a sealing ring mode;
the first liquid line 207 is provided with a plurality of first liquid nozzles 205, and the second liquid line 208 is provided with a plurality of second liquid nozzles 206. The number of the first liquid nozzles 205 and the second liquid nozzles 206 is the same, and the positions of the first liquid nozzles 205 and the second liquid nozzles 206 correspond. The first liquid nozzle 205 and the second liquid nozzle 206 are coaxially and concentrically arranged in opposite directions, and concentric with the second rotating shaft 201, and the axial mounting positions of the first liquid nozzle 205 and the second liquid nozzle 206 are symmetrical about the center line of the thickness of the second wire mesh 204.
In the present application, unless otherwise indicated, CO is used 2 The mixed waste gas is obtained by simulating the flue gas of the thermal power plant through a flue gas simulation distribution part. As shown in FIG. 1, the final pressure of the gas buffer tank (20L) was first set to 0.1MPa (gauge pressure), and then 79.9% nitrogen, 15.0% carbon dioxide, 0.1% sulfur dioxide and 5.0% air (volume fraction) were sequentially charged by an air compressor by adjusting the corresponding gas flow meters according to the pressure and volume of the gas buffer tankA gas buffer tank for obtaining CO 2 Mixing exhaust gas, CO 2 The mixed waste gas passes through a gas flowmeter, then the gas component analysis of the mixed gas is completed through a smoke analyzer by a two-way valve, a three-way valve and a regulating valve, and then CO is added 2 The mixed exhaust gas is passed into a gas-liquid cross-flow supergravity reactor 100.
In the application, unless otherwise indicated, the solid waste slurry is prepared by crushing and grinding solid waste, adding deionized water and stirring; the liquid-solid ratio is 15:1 (L/Kg).
In the present application, unless otherwise specified, the solid waste is crushed and ground, and the mass percent (%) of the chemical components of the alkaline solid waste is measured by an X-ray fluorescence spectrometer is shown in table 1:
TABLE 1
Example 1
As shown in fig. 1, a CO 2 The method for absorbing and desorbing solid waste resources comprises setting the hypergravity factors of a gas-liquid cross-flow hypergravity reaction system and an impinging stream hypergravity reaction system as 100, and setting the two hypergravity reaction systems to be normal pressure and normal temperature, wherein the method specifically comprises the following steps:
(1) CO is processed by 2 Mixing the exhaust gas at 100m 3 The gas flow rate of/h is injected into the gas-liquid cross flow hypergravity reactor 100 from the lower gas inlet, the first rotating body 105 is driven by a first driving source to rotate at high speed, the diethanolamine solution with the mass concentration of 40% is preheated to 40 ℃ and uniformly sprayed to the edge of the first wire mesh 107 from the upper liquid inlet through the liquid distributor 102, the liquid is sheared into liquid forms of micro nano scale such as liquid drops, liquid wires or liquid films under the action of centrifugal force, and moves from the inner edge to the outer edge of the first wire mesh 107 along the radial direction of the first wire mesh 107, so that CO is realized 2 The mixed waste gas contacts with amine absorbent diethanolamine in a cross flow way, the liquid falls down after hitting the inner wall of the first shell 108 and is discharged from the first liquid outlet 110 positioned at the bottom, thus obtaining the absorption and trapping of CO 2 Amine absorption liquid of (2);the gas which is not absorbed and trapped is discharged from a gas outlet 106 at the upper part of the shell and enters a detection part of the smoke analyzer through a three-way valve for component analysis;
during this process, diethanolamine and dissolved CO 2 React to form (CH) 2 CH 2 OH) 2 NCOOH, the reaction is as follows:
；
but (CH) 2 CH 2 OH) 2 NCOOH is unstable and the following reactions occur in the reaction system:
。
along with CO 2 The pH of the reaction system is continuously reduced by continuously introducing, and the carbamate ((CH) 2 CH 2 OH) 2 NCOO - ) Will react with proton ions to form bicarbonate (HCO) 3 - ) The reaction is as follows:
。
(2) Absorption and capture of CO 2 The amine absorption liquid (liquid 1) and the carbide slag slurry (liquid 2) are simultaneously mixed at a ratio of 1.5m 3 The liquid flow rate/h is pumped into the impinging stream supergravity reactor 200 from the upper part through a lift pump, is measured through a liquid flowmeter and is sprayed out through a second liquid nozzle 206, and primary rapid collision, mixing and reaction are carried out in an impinging zone. Then the liquid moves from inside to outside along the radial direction to enter into high-speed collision and shearing, and the fluids are subjected to secondary deep uniform mixing and reaction. Thus CO 2 The amine absorbent is transferred to the solid waste slurry to be fixed into carbonate, and the amine absorbent is regenerated. The liquid after the reaction is thrown out, flows to a second liquid outlet 210 along the inner wall of the second housing 209, and is discharged;
in this process, the reaction takes place as follows:
。
(3) The discharged liquid is discharged into a liquid storage tank, a solid product and an amine absorbent regenerated liquid are obtained through sedimentation and separation, the amine absorbent is regenerated and returned to the top of the gas-liquid cross-flow hypergravity reactor again for the next round of CO 2 Absorption cycle, solid precipitate (CaCO) obtained 3 And MgCO 3 ) And the product can be reused as a recycling product after dehydration and drying.
Example 2
Substantially the same as in example 1, the difference is that: the amine absorbent is N-methyl diethanolamine.
Test example 1
Based on example 1, different solid waste fixation CO was explored 2 And (3) carrying out thermogravimetric analysis on solid products obtained by sedimentation and separation in the liquid storage tank: the solid product was dried in an oven at 105℃to remove surface moisture and then subjected to thermogravimetric analysis with a temperature program set to N at a flow rate of 19.8mL/min 2 In the atmosphere, the temperature is raised at a rate of 10 ℃/min within the range of 50 ℃ to 950 ℃. Experience shows that the pyrolysis temperature of carbonate is mainly 500-850 ℃, and the solid waste is fixed with CO 2 The amount of (2) can be obtained by reducing the amount of carbonate in the obtained solid product, and the result is shown in FIG. 5.
As can be seen from fig. 5, the obvious weight loss occurring in the range of 600-900 ℃ is caused by the decomposition of carbonates, and under the same operating condition, the mass of the carbonates obtained by the reaction and the carbon fixation of carbide slag is more than that of the other two types of solid wastes, which is related to the components of the alkaline solid wastes, and the higher the CaO and MgO content of the components, the higher the carbon fixation capability. Under the running condition provided by the application, carbide slag can fix carbonThe force is about that per ton of carbide slag can fix CO 2 About 350kg.
Test example 2
Based on example 1, different gas flows and CO were investigated 2 The relationship between the absorptivity is shown in fig. 6. As can be seen from FIG. 6, the gas flow rate is relative to CO 2 The absorption rate has a great influence, and as the gas flow rate increases, CO 2 The absorption rate decreases, because as the amount of intake air increases, on the one hand the gas velocity increases, the residence time of the gas in the rotating packed bed decreases, the contact time of the mixed gas with the incoming amine absorbent decreases, and the absorption rate decreases. The gas flow rate of the present application is set to 50m in consideration of both the treatment capacity and the absorption efficiency 3 /h-150m 3 /h。
Test example 3
Based on example 1, different amine absorber concentrations and CO were investigated 2 The relationship between the absorptivity is shown in fig. 7. As can be seen from fig. 7, the higher the concentration of diethanolamine, the better the absorption effect, but the higher the running cost, and the mass concentration of amine absorbent is 30% -40% in comprehensive consideration during engineering running.
Test example 4
Based on example 1, different hypergravity factors and CO were explored 2 The relationship between the absorptivity is shown in fig. 8. As can be seen from FIG. 8, the supergravity factor is used to measure the strength of the supergravity field, CO 2 The absorption rate is increased along with the increase of the supergravity factor, which is due to the fact that the supergravity reactor strengthens the gas-liquid phase mass transfer, the supergravity factor increases the capability of filling materials to cut amine absorbent, thereby increasing the contact area of the gas and the liquid, and accelerating the update rate of the liquid surface, which is beneficial to CO 2 And amine absorbers. However, the increase of the supergravity factor leads to the increase of the power of the motor and the increase of the energy consumption, so that the proper choice of the supergravity factor according to the industrial application condition is important, and the optimal supergravity factor is set to be about 100 in the example. From the figure, it can be seen that CO 2 The absorptivity reaches more than 96%. Similarly, the change between the reaction efficiency and the hypergravity factor between the liquid and the liquid in the impinging stream hypergravity reaction systemThe relationship is the same as above.
Test example 5
Based on example 1, cyclic regeneration of amine-based absorbent was investigated, and the results are shown in fig. 9. As can be seen from FIG. 9, the continuous cycle was run 10 times, and it can be seen that the diethanolamine absorbent still had a higher CO after regeneration in the first 5 cycles 2 Absorption rate (85% or more).
To sum up, the CO of the application 2 The method for absorbing and desorbing and recycling the solid waste can still stably operate with high absorption rate, realize cyclic loading and higher regeneration efficiency in the continuous cyclic absorption-fixation process, and realize the reduction of the amine absorbent and recycling of the solid waste and the CO in the flue gas 2 Emission reduction, running cost saving and CO realization 2 Is fixed in resource.
It is apparent that the above examples are given by way of illustration only and are not limiting of the embodiments. Other variations and modifications of the present application will be apparent to those of ordinary skill in the art in light of the foregoing description. It is not necessary here nor is it exhaustive of all embodiments. And obvious variations or modifications thereof are contemplated as falling within the scope of the present application.
Claims (5)
1. CO (carbon monoxide) 2 The method for absorbing and desorbing and recycling the solid waste is characterized by taking a recycling system as a generating device, wherein the recycling system comprises a gas-liquid cross-flow hypergravity reactor and an impinging stream hypergravity reactor, and the gas-liquid cross-flow hypergravity reactor is used for recycling CO 2 The mixed waste gas is quickly transferred into amine absorbent solution, and the impinging stream supergravity reactor is used for converting CO-containing gas 2 Fully contacting the amine absorption liquid and the solid waste slurry; the method comprises the following steps:
(1) CO is processed by 2 Injecting mixed waste gas into the gas-liquid cross-flow hypergravity reactor from the lower part, and utilizing amine absorbent solution at the upper part of the gas-liquid cross-flow hypergravity reactor to perform CO 2 The mixed waste gas is trapped and shearedThe CO is obtained by reaction 2 Amine absorption liquid of (2); the amine absorbent in the amine absorbent solution is diethanolamine and/or N-methyldiethanolamine; the CO 2 The gas flow rate of the mixed waste gas is 50m 3 /h-150m 3 /h; the mass concentration of the amine absorbent solution is 30% -50%;
(2) The CO-containing component in the step (1) 2 Pumping the amine absorption liquid and solid waste slurry into the impinging stream hypergravity reactor from the upper part, and obtaining mixed liquid through collision, mixing and reaction, wherein the mixed liquid is discharged and separated to realize CO 2 The absorption and desorption have the resource utilization of solid waste; the solid waste in the solid waste slurry is one or more of carbide slag, shale fly ash and steel slag;
the hypergravity factors of the gas-liquid cross flow hypergravity reactor and the impinging stream hypergravity reactor are 80-120.
2. The CO according to claim 1 2 The method for absorbing and desorbing and recycling the solid waste is characterized by comprising the following steps of: in step (1), the CO 2 The components of the mixed waste gas comprise carbon dioxide, nitrogen and sulfur dioxide; the volume ratio of the carbon dioxide to the nitrogen to the sulfur dioxide is 15:79.9:0.1.
3. the CO according to claim 1 2 The method for absorbing and desorbing and recycling the solid waste is characterized by comprising the following steps of: in the step (2), the solid waste slurry has a liquid-solid ratio of 10-20:1.
4. the CO according to claim 1 2 The method for absorbing and desorbing and recycling the solid waste is characterized by comprising the following steps of: in step (2), the CO-containing gas is 2 The liquid flow rate of the amine absorption liquid is 1.5m 3 /h-1.8m 3 /h。
5. The CO according to claim 1 2 The method for absorbing and desorbing and recycling the solid waste is characterized by comprising the following steps of: in step (2), the solids are discardedThe liquid flow rate of the slurry was 1.5m 3 /h-1.8m 3 /h。
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| CN102580462A (en) * | 2011-01-12 | 2012-07-18 | 北京化工大学 | Novel method for capturing and separating carbon dioxide |
| CN103007721A (en) * | 2012-11-26 | 2013-04-03 | 东南大学 | Ammonia circulation-based method and device for carbonating fixation of CO2 in coal-fired flue gas |
| CN109999648A (en) * | 2019-03-14 | 2019-07-12 | 中北大学 | A kind of method that hypergravity synergic nano fluid technique strengthens trapping sour gas |
| CN111298616A (en) * | 2019-12-17 | 2020-06-19 | 四川大学 | Desulfurized slag regenerated CO2Method for trapping solvent |
| CN114570204A (en) * | 2022-03-14 | 2022-06-03 | 昆明理工大学 | Method for dealkalizing and soil-working red mud mediated by organic amine |
| CN218393035U (en) * | 2022-07-18 | 2023-01-31 | 超重力股份有限公司 | Sodium bicarbonate production system |
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2023
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Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102580462A (en) * | 2011-01-12 | 2012-07-18 | 北京化工大学 | Novel method for capturing and separating carbon dioxide |
| CN103007721A (en) * | 2012-11-26 | 2013-04-03 | 东南大学 | Ammonia circulation-based method and device for carbonating fixation of CO2 in coal-fired flue gas |
| CN109999648A (en) * | 2019-03-14 | 2019-07-12 | 中北大学 | A kind of method that hypergravity synergic nano fluid technique strengthens trapping sour gas |
| CN111298616A (en) * | 2019-12-17 | 2020-06-19 | 四川大学 | Desulfurized slag regenerated CO2Method for trapping solvent |
| CN114570204A (en) * | 2022-03-14 | 2022-06-03 | 昆明理工大学 | Method for dealkalizing and soil-working red mud mediated by organic amine |
| CN218393035U (en) * | 2022-07-18 | 2023-01-31 | 超重力股份有限公司 | Sodium bicarbonate production system |
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