CN115945054A - CO (carbon monoxide) 2 Method for absorbing, desorbing and utilizing solid waste as resource - Google Patents
CO (carbon monoxide) 2 Method for absorbing, desorbing and utilizing solid waste as resource Download PDFInfo
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- CN115945054A CN115945054A CN202310245241.1A CN202310245241A CN115945054A CN 115945054 A CN115945054 A CN 115945054A CN 202310245241 A CN202310245241 A CN 202310245241A CN 115945054 A CN115945054 A CN 115945054A
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Abstract
The invention relates to CO 2 A method for absorbing, desorbing and utilizing solid waste as resources, which relates to CO 2 The technical field of treatment. The method comprises the steps of introducing CO 2 Injecting the mixed waste gas into a gas-liquid cross-flow hypergravity reactor from the lower part, and reacting CO by using an amine absorbent solution at the upper part of the gas-liquid cross-flow hypergravity reactor 2 Collecting, shearing and reacting the mixed waste gas to obtain CO 2 The amine-based absorption liquid of (1); will contain CO 2 The amine absorption liquid and the solid waste slurry are pumped into an impinging stream hypergravity reactor from the upper part, mixed liquid is obtained through collision, mixing and reaction, and the CO is discharged and separated from the mixed liquid 2 Absorption and desorption as well as solid waste resourceAnd (4) chemical utilization. The method realizes CO 2 The mixed waste gas contacts with the amine absorbent solution in a gas-liquid cross-flow hypergravity reactor rotating at a high speed in a cross-flow manner, so that 90-98 percent of CO can be obtained 2 And (4) absorbing and trapping. Trapped CO 2 And (4) discharging the mixed waste gas or performing desulfurization and denitrification treatment according to the condition.
Description
Technical Field
The invention relates to CO 2 The technical field of treatment, in particular to CO 2 A method for absorbing and desorbing as well as utilizing solid wastes as resources.
Background
With the development of human society, the material energy is consumed in large quantity, and a large amount of CO is generated 2 Causing global climate problems to change dramatically. At present, post-combustion CO 2 The capture technique is one of the most commonly used CO 2 Emission reduction technique, post combustion CO 2 The trapping technology is used for separating and recovering CO in flue gas by using various technical means after fuel combustion 2 CO after combustion, according to the separation method 2 The trapping technique can be divided into: chemical absorption method using CO, solid adsorption method, membrane separation method, temperature-based phase separation method, and the like 2 And chemical absorbent to remove CO 2 Technology for selectively separating gas from flue gas, which is a continuous cyclic process including 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 Formation of CO 2 And (4) enriching the liquid. Subsequent CO 2 The rich solution releases the absorbed CO at higher temperature in the desorption tower 2 And regeneration of the absorbent is realized. The process can efficiently remove CO from flue gas 2 And production of high purity CO 2 CO in flue gas 2 Can reach 99%, and nevertheless, the process still faces great challenges of high energy consumption and high investment running cost.
Membrane separation technology for CO 2 The separation of (3) has high separation cost, and the stability and selectivity of the separation are required to be further optimized. CO Using solid Material 2 The trapping has many advantages such as less by-products generated during the recycling process, easy disposal of the waste solid adsorbent, and the like. However, the amount of adsorption is low, and the adsorption efficiency is low.
In addition, with the rapid development of industrial society, some solid wastes rich in metal oxide components such as calcium, magnesium and the likeThe solid wastes are generally alkaline, the leaching of heavy metal ions in the components of the solid wastes can cause great pollution to land and underground water resources, and the solid wastes comprise steelmaking waste residues, fly ashes of coal-fired power plants, fly ashes left after the incineration of wastes, shale fly ashes, carbide slag, waste building materials, tailings in certain metal smelting processes such as serpentine tailings and the like, the metal elements in the solid wastes are rich, and a large amount of calcium-magnesium metal oxides can be provided, such as CaO/MgO in the steelmaking solid waste residues accounting for about 30-60% of the whole mass content, caO in the fly ashes of the coal-fired power plants accounting for about 65% of the mass content, caO in the wastes left after the incineration of municipal solid wastes accounting for about 30% of the mass content, and many of the wastes are obtained after a carbonation process, the reaction activity is high, and the wastes are used for CO through a reaction, so as to obtain the calcium-magnesium calcium carbonate calcium-magnesium-calcium carbonate composite material 2 The emission reduction process can not only reduce the pollution of solid wastes to the environment, but also fix CO 2 。
At present in CO 2 In the treatment technique, CO 2 The capture and sequestration of (A) is the technical focus, and the CO is related to 2 The effect of emission control. Among the above trapping technologies, the chemical absorption method is the one with the highest trapping efficiency and the best applicability, but the purified CO obtained after trapping and purification is relatively pure 2 How to safely fix the carbon dioxide in order to isolate the carbon dioxide from the atmosphere for a long time to achieve the aim of relieving the greenhouse effect, how to reduce the consumption of the chemical absorbent and improve the recycling rate of the chemical absorbent become the current CO 2 The emission reduction technology focuses on the problem.
Disclosure of Invention
Therefore, the technical problem to be solved by the invention is to overcome the CO capture by a chemical absorption method in the prior art 2 The chemical absorbent can not be recycled and has large dosage, and simultaneously, the problem of directly fixing CO by solid waste is solved 2 Low fixation rate, low efficiency and slow reaction.
In order to solve the technical problem, the invention provides CO 2 Absorption and desorption as well as solid waste resourceThe chemical utilization method comprises two processes: firstly, in a first gas-liquid cross-flow hypergravity reactor, an amine absorbent is adopted to absorb CO 2 Chemical regeneration is achieved by precipitation reaction (change in pH); then containing CO 2 The amine absorption liquid enters an impinging stream hypergravity reactor to react with solid waste slurry, and CO is neutralized by acid and alkali according to the principle of neutralization reaction 2 With CaCO 3 And MgCO 3 Is fixed.
The invention aims to provide CO 2 A method for absorbing, desorbing and utilizing solid wastes as resources takes a resource utilization system as a generating device, the resource utilization 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 utilizing CO 2 The mixed waste gas is quickly transferred into amine absorbent solution, and the impinging stream hypergravity reactor is used for containing CO 2 The amine absorption liquid is fully contacted with the solid waste slurry; the method comprises the following steps:
(1) Introducing CO 2 Injecting mixed waste gas into the gas-liquid cross-flow hypergravity reactor from the lower part, and reacting CO by using amine absorbent solution at the upper part of the gas-liquid cross-flow hypergravity reactor 2 The mixed waste gas is collected, sheared and reacted to obtain CO 2 The amine-based absorption liquid of (1); the amine absorbent in the amine absorbent solution is diethanolamine and/or N-methyldiethanolamine;
(2) The CO contained in the step (1) 2 The amine absorption liquid and the solid waste slurry are pumped into the impinging stream hypergravity reactor from the upper part, mixed liquid is obtained through collision, mixing and reaction, and the mixed liquid is discharged and separated to realize CO 2 Absorption and desorption are realized, and solid waste is recycled; 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 invention, the hypergravity factors of the gas-liquid cross-flow hypergravity reactor and the impinging-flow hypergravity reactor are both 80 to 120.
In one embodiment of the present invention, in step (1), theCO 2 The mixed exhaust gas comprises flue gas.
In one embodiment of the present invention, 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 invention, in step (1), the CO 2 The gas flow of the mixed waste gas is 50m 3 /h-150m 3 /h。
In one embodiment of the present invention, in the step (1), the mass concentration of the amine absorbent solution is 30% to 50%; the temperature of the amine absorbent solution is 40-50 ℃, and the temperature is closer to the temperature of flue gas.
In one embodiment of the present invention, in the step (2), the solid waste is rich in metal oxide components such as calcium and magnesium, has high content of calcium, has high reactivity, and is used as CO 2 Fixed raw material, high CO 2 The potential of sealing and storing, and the final product obtained after sealing and storing can be harmlessly treated and recycled in roadbeds or other building materials, so that energy conservation and emission reduction and comprehensive utilization of solid waste resources are realized.
In one embodiment of the present invention, in the step (2), the solid waste slurry has a liquid-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 (a) increases the chance of the ions coming into contact with each other, thereby increasing the reaction rate. When the solid waste is added into deionized water, hydration reaction occurs to convert CaO and MgO into Ca (OH) 2 、Mg(OH) 2 (ii) a Then Ca (OH) 2 、Mg(OH) 2 Ca obtained by dissolution 2+ 、Mg 2+ And 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 invention, in the step (2), the CO-containing compound 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 invention, in the 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 invention has the following advantages:
(1) The resource utilization method realizes CO 2 The mixed waste gas contacts with the amine absorbent in a gas-liquid cross-flow hypergravity reactor rotating at a high speed in a cross-flow manner, so that 90 to 98 percent of CO can be obtained 2 And (4) absorbing and trapping. Trapped CO 2 And (4) discharging the mixed waste gas or performing desulfurization and denitrification treatment according to the condition. In the process, the micro-nano-scale liquid drops, liquid filaments or liquid films formed by the amine absorbent have extremely large interphase area, and the surfaces are quickly updated under the action of the supergravity, so that the gas-liquid interphase transfer rate is greatly enhanced, and the CO is improved 2 Absorption and collection efficiency.
(2) The resource utilization method of the invention utilizes the gas-liquid cross-flow hypergravity reactor to strengthen CO 2 The process of mixed waste gas is fast shifted to the liquid phase from gaseous phase, is showing and is promoting absorption rate and purifying effect. The high dispersion of the amine absorbent by the supergravity can reduce the using amount of the absorbent, reduce the gas phase resistance of the equipment and save the power consumption of a pump and a fan.
(3) According to the resource utilization method, the filler in the impinging stream hypergravity reactor is utilized to shear the liquid into a liquid form with a micro-nano scale, so that the updating rate of the liquid surface is enhanced, the turbulence of the liquid is increased, and the separation of a boundary layer is promoted, so that the liquid-liquid contact process is obviously enhanced, and the precipitation reaction efficiency is improved.
Drawings
In order that the present invention may be more readily and clearly understood, reference will now be made in detail to the present invention, examples of which are illustrated in the accompanying drawings.
FIG. 1 is a CO of the present invention 2 A process flow chart of absorption and desorption and solid waste resource utilization.
FIG. 2 is a schematic of a gas-liquid cross-flow hypergravity reactor of the present invention.
FIG. 3 is a schematic diagram of a liquid distributor in a gas-liquid cross-flow hypergravity reactor of the present invention.
FIG. 4 is a schematic of an impinging stream hypergravity reactor of the present invention.
FIG. 5 is the result of thermogravimetric analysis of the solid product of test example 1 of the present invention.
FIG. 6 is gas flow vs. CO for test example 2 of the present invention 2 Graph of the effect of absorbance.
FIG. 7 is a graph of amine absorbent concentration versus CO for test example 3 of the present invention 2 Graph of the effect of absorbance.
FIG. 8 shows the hypergravity factor vs. CO of test example 4 of the present invention 2 Graph of the effect of absorbance.
FIG. 9 is a graph showing the cyclic regeneration of the amine-based absorbent of test example 5 of the present invention.
The specification reference numbers indicate: 100-gas-liquid cross-flow hypergravity reactor, 101-first rotating shaft, 102-liquid distributor, 1021-water outlet, 103-first rotating joint, 104-gas seal, 105-first rotating body, 106-gas outlet, 107-first wire mesh, 108-first shell, 109-first shaft seal, 110-first liquid outlet, 200-impinging flow hypergravity 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 and 211-second shaft seal.
Detailed Description
The present invention is further described below in conjunction with the following figures and specific examples so that those skilled in the art may better understand the present invention and practice it, but the examples are not intended to limit the present invention.
In the present invention, unless otherwise specified, CO 2 The formula for calculating the absorption rate is as follows:CO 2 absorption rate = (C in V in -C out V out )/C in V in (ii) a Wherein the content of the first and second substances,C in 、C out is CO at the inlet and outlet of the reaction system 2 The volume concentration (%),V in 、V out is the inlet and outlet gas flow (m) of the reaction system 3 /h）。
In the present invention, unless otherwise specified, the hypergravity factor calculation formula is:
(ii) a Wherein n is the rotating speed of the rotor, r/min; r-radius of rotor, m;
in the present invention, unless otherwise specified, CO 2 The method for absorbing, desorbing and utilizing solid waste as resources takes a resource utilization system as a generating device as shown in figure 1, and mainly comprises five modules: the device comprises a flue gas simulation gas distribution part, a gas-liquid cross-flow hypergravity reactor, an impinging flow hypergravity reactor, a liquid storage solid-liquid separation part and a flue gas analysis and detection part. The gas distribution simulating part consists of various gas bottles, an air compressor, a gas buffer tank, a gas flowmeter, a two-way valve and a three-way valve.
In the present invention, unless otherwise stated, the gas-liquid cross-flow hypergravity reactor 100 is communicated with a gas buffer tank of a flue gas simulation gas distribution part, and the specific structure is shown in fig. 2-3: it comprises a liquid distributor 102, a first rotating body 105 and a first casing 108, the first casing 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 rotating body 105 has a first wire mesh 107 and the first rotating body 105 is disposed inside the first casing 108; a hermetic seal 104, the hermetic seal 104 being a sealing device for sealing the gap of the rotating shaft with compressed air so as not to 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 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 rotating joint 103;
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, that is, 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 disk and a first lower rotating disk, and the first wire mesh 107 is disposed on the first upper rotating disk and the first lower rotating disk; the first upper rotating disc and the first lower rotating disc are both provided with first channels for the penetration of the liquid distributors 102. The first wire mesh 107 is a filler, and the filler is an annular disc-shaped filler formed by winding, overlapping and assembling a plurality of parallel corrugated wire meshes.
In the present invention, unless otherwise stated, the impinging stream hypergravity reactor 200 is connected to the gas-liquid cross-flow hypergravity reactor 100, and the specific structure is shown in fig. 4; it comprises a second rotation body 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 rotating body 203 is provided with a second wire mesh 204 and the second rotating body 203 is arranged in a second housing 209, the first liquid pipeline 207 is communicated with the first liquid outlet 110, and the second liquid pipeline 208 introduces and sprays liquid;
the second rotating body 203 comprises a second upper rotating disc and a second lower rotating disc, and the second wire mesh 204 is arranged on the second upper rotating disc and the second lower rotating disc; the second upper rotary table and the second lower rotary table are provided with second channels 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. The second wire mesh 204 is a filler, and the filler is an annular disc-shaped filler formed by winding, overlapping and assembling 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 an output end of a driving source such as a commercially available motor. A second shaft seal 211 is arranged at the joint of one end of the second rotating shaft 201 and the second shell 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 ejection nozzle 205 and the second liquid ejection nozzle 206 are coaxially, concentrically and reversely arranged, concentrically with the second rotary shaft 201, and the axial installation positions of the first liquid ejection nozzle 205 and the second liquid ejection nozzle 206 are symmetrical with respect to the center line of the thickness of the second wire mesh 204.
In the present invention, unless otherwise specified, CO is used 2 The mixed waste gas is obtained by simulating flue gas of a thermal power plant through a flue gas simulation gas distribution part. As shown in FIG. 1, the final pressure of the gas buffer tank (20L) is set to 0.1MPa (gauge pressure), according to the pressure and volume of the gas buffer tank, then 79.9% nitrogen, 15.0% carbon dioxide, 0.1% sulfur dioxide and 5.0% air (volume fraction) are sequentially filled into the gas buffer tank through an air compressor by adjusting the corresponding gas flow meter, and CO is obtained 2 Mixed exhaust gas, CO 2 The mixed waste gas passes through a gas flowmeter, then passes through a two-way valve, a three-way valve and an adjusting valve to complete the gas component analysis of the mixed gas through a flue gas analyzer, and then CO is mixed 2 The mixed waste gas is introduced into the gas-liquid cross-flow hypergravity reactor 100.
In the invention, unless otherwise stated, the solid waste slurry is prepared by grinding solid waste, adding deionized water and stirring; the liquid-solid ratio is 15:1 (L/Kg).
In the present invention, unless otherwise specified, the solid waste was pulverized and ground, and the mass percentages (%) of the chemical components of the alkaline solid waste measured by an X-ray fluorescence spectrometer are shown in table 1:
TABLE 1
Example 1
As shown in FIG. 1, a CO 2 The method for absorption desorption and solid waste resource utilization is characterized in that the hypergravity factors of a gas-liquid cross-flow hypergravity reaction system and an impinging stream hypergravity reaction system are set to be 100, and the two hypergravity reaction systemsThe method is under normal pressure and normal temperature, and specifically comprises the following steps:
(1) Introducing CO 2 Mixing exhaust gas at 100m 3 The gas flow of/h is injected into the gas-liquid cross-flow hypergravity reactor 100 from the gas inlet at the lower part, the first rotating body 105 is driven by the first driving source to rotate at high speed, the diethanolamine solution with the mass concentration of 40 percent is preheated to 40 ℃, and is uniformly sprayed to the edge of the first wire mesh 107 from the liquid inlet at the upper part through the liquid distributor 102, under the action of centrifugal force, the liquid is sheared into liquid forms with micro-nano sizes such as liquid drops, liquid wires or liquid films, 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 manner, the liquid falls after contacting the inner wall of the first shell 108 and is discharged from a first liquid outlet 110 at the bottom, and CO is absorbed and trapped 2 The amine-based absorption liquid of (1); 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 a flue gas analyzer through a three-way valve to carry out component analysis;
in this process, diethanolamine with dissolved CO 2 Is reacted 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:
with CO 2 Continuously introducing the mixture, continuously reducing the pH value of the reaction system, and obtaining 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) Absorb and trap CO 2 The amine absorption liquid (liquid 1) and the carbide slag slurry (liquid 2) are simultaneously 1.5m 3 The flow rate of the liquid/h is pumped into the impinging stream hypergravity reactor 200 from the upper part through a lift pump, is metered by a liquid flow meter and then is sprayed out through a second liquid nozzle 206, and the initial rapid collision, mixing and reaction are carried out in an impinging area. Then the liquid moves from inside to outside along the radial direction and enters high-speed collision and shearing, and secondary deep uniform mixing and reaction are carried out between the fluids. Thus CO 2 The amine absorbent is transferred to solid waste slurry from the amine absorbent to be fixed into carbonate, and the amine absorbent is regenerated. Finally, the liquid after the reaction is thrown out and flows to a second liquid outlet 210 along the inner wall of the second shell 209 to discharge the liquid;
in this process, the reactions that occur are as follows:
(3) Discharging the discharged liquid into a liquid storage tank, obtaining a solid product and an amine absorbent regeneration liquid through sedimentation separation, and regenerating the amine absorbent to return to the top of the gas-liquid cross-flow supergravity reactor again for next round of CO 2 Absorption cycle, solid precipitate (CaCO) obtained 3 And MgCO 3 ) Can be reused as a resource product after dehydration and drying.
Example 2
Basically the same as example 1, except that: the amine absorbent is N-methyldiethanolamine.
Test example 1
Based on example 1, different solid waste fixed CO was explored 2 And (3) performing thermogravimetric analysis on a solid product obtained by settling separation in a liquid storage tank:drying the solid product in a 105 ℃ oven to remove surface moisture, and performing thermal gravimetric analysis, wherein the temperature rise program is set to be N at the flow rate of 19.8mL/min 2 In the atmosphere, the temperature is increased at the rate of 10 ℃/min within the range of 50-950 ℃. Experience shows that the pyrolysis temperature of the carbonate is mainly 500-850 ℃, and the solid waste fixes CO 2 The amount of (c) can be obtained by reducing the amount of carbonate in the obtained solid product, and the results are shown in FIG. 5.
It can be seen from fig. 5 that the significant weight loss occurring in the range of 600-900 ℃ is caused by the decomposition of carbonates, and under the same operating conditions, the mass of carbonates obtained by carbide slag through reaction carbon fixation is more than that of other two types of solid wastes, which is related to the components of alkaline solid wastes, and the higher the contents of CaO and MgO in the components, the higher the carbon fixation capacity. Under the operation condition provided by the invention, the carbon fixation capacity of the carbide slag is about the capability of fixing CO per ton of the carbide slag 2 About 350kg.
Test example 2
Based on example 1, different gas flows and CO were explored 2 The relationship between the absorbances, the results are shown in fig. 6. As can be seen from FIG. 6, gas flow vs. CO 2 The absorption rate has a greater influence, with increasing gas flow, CO 2 The absorption rate is reduced because the gas velocity is increased with the increase of the gas inflow, the retention time of the gas in the rotating packed bed is shortened, the contact time of the mixed gas and the entering amine absorbent is reduced, and the absorption rate is reduced. The gas flow rate is set to 50m in the present invention in consideration of both the comprehensive treatment capacity and the absorption efficiency 3 /h-150m 3 /h。
Test example 3
Based on example 1, different amine absorbent concentrations and CO were explored 2 The relationship between the absorbances, the results are shown in fig. 7. As can be seen from FIG. 7, the higher the concentration of diethanolamine is, the better the absorption effect is, but the higher the running cost is, and comprehensively considering, the mass concentration of the amine absorbent is 30% -40% during engineering running.
Test example 4
Based on example 1, different hypergravity factors and CO were investigated 2 Relationship between absorptance, knotAs shown in fig. 8. As can be seen from FIG. 8, the hypergravity factor is used to measure the intensity of the hypergravity field, CO 2 The absorption rate is increased along with the increase of the hypergravity factor, which is the result of the strengthened gas-liquid interphase mass transfer of the hypergravity reactor, the capacity of the filler for cutting the amine absorbent is enhanced due to the increase of the hypergravity factor, the contact area of the gas and the liquid is further increased, and the updating rate of the liquid surface is accelerated, so that the CO absorption rate is favorably increased 2 And amine absorbents. However, since increasing the hypergravity factor leads to an increase in the power of the motor and an increase in the power consumption, it is important to appropriately select the appropriate hypergravity factor according to the industrial application conditions, and in this example, the optimal hypergravity factor is set to about 100. As can be seen from the figure, CO 2 The absorption rate reaches more than 96 percent. Similarly, the reaction efficiency between liquid and liquid in the impinging stream hypergravity reaction system is the same as the variation relationship between the hypergravity factors.
Test example 5
The cyclic regeneration of the amine-based absorbent was explored based on example 1 and the results are shown in figure 9. As can be seen from FIG. 9, the continuous cycle was run for 10 times, and it can be seen that the diethanolamine absorbent still has high CO after regeneration in the first 5 cycles 2 Absorption rate (more than 85%).
In summary, the CO of the present application 2 The method for absorption desorption and solid waste resource utilization can still stably run at high absorption rate and realize cyclic loading and higher regeneration efficiency in the continuous cyclic absorption-fixation process of the amine absorbent, realizes the reduction of the amine absorbent and the resource utilization of solid waste, and realizes the CO in flue gas 2 Reduce emission, save the operation cost and realize CO 2 And (4) resource fixation.
It should be understood that the above examples are only for clarity of illustration and are not intended to limit the embodiments. Other variations and modifications will be apparent to persons skilled in the art in light of the above description. And are neither required nor exhaustive of all embodiments. And obvious variations or modifications of the invention may be made without departing from the spirit or scope of the invention.
Claims (8)
1. CO (carbon monoxide) 2 The method for absorbing, desorbing and utilizing solid waste as resource is characterized in that a resource utilization system is taken as a generating device, the resource utilization 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 hypergravity reactor is used for containing CO 2 The amine absorption liquid is fully contacted with the solid waste slurry; the method comprises the following steps:
(1) Introducing CO 2 Injecting mixed waste gas into the gas-liquid cross-flow hypergravity reactor from the lower part, and reacting CO by using amine absorbent solution at the upper part of the gas-liquid cross-flow hypergravity reactor 2 The mixed waste gas is collected, sheared and reacted to obtain CO 2 The amine-based absorption liquid of (1); the amine absorbent in the amine absorbent solution is diethanolamine and/or N-methyldiethanolamine;
(2) The CO contained in the step (1) 2 The amine absorption liquid and the solid waste slurry are pumped into the impinging stream hypergravity reactor from the upper part, mixed liquid is obtained through collision, mixing and reaction, and the mixed liquid is discharged and separated to realize CO 2 Absorption and desorption are realized, and solid waste is recycled; the solid waste in the solid waste slurry is one or more of carbide slag, shale fly ash and steel slag.
2. CO according to claim 1 2 The method for absorption desorption and solid waste resource utilization is characterized by comprising the following steps: the hypergravity factors of the gas-liquid cross-flow hypergravity reactor and the impinging-flow hypergravity reactor are both 80-120.
3. CO according to claim 1 2 The method for absorption desorption and solid waste resource utilization is characterized by comprising the following steps: in step (1), the CO 2 The components of the mixed waste gas comprise carbon dioxide, nitrogen and sulfur dioxide; the carbon dioxide, nitrogen and sulfur dioxideIs 15:79.9:0.1.
4. CO according to claim 1 2 The method for absorption desorption and solid waste resource utilization is characterized by comprising the following steps: in step (1), the CO 2 The gas flow of the mixed waste gas is 50m 3 /h-150m 3 /h。
5. CO according to claim 1 2 The method for absorption desorption and solid waste resource utilization is characterized by comprising the following steps: in the step (1), the mass concentration of the amine absorbent solution is 30-50%.
6. CO according to claim 1 2 The method for absorption desorption and solid waste resource utilization is characterized by comprising the following steps: in the step (2), the liquid-solid ratio of the solid waste slurry is 10-20:1.
7. CO according to claim 1 2 The method for absorption desorption and solid waste resource utilization is characterized by comprising the following steps: in the step (2), the CO-containing 2 The liquid flow rate of the amine absorption liquid is 1.5m 3 /h-1.8m 3 /h。
8. CO according to claim 1 2 The method for absorption desorption and solid waste resource utilization is characterized by comprising the following steps: in the step (2), the liquid flow rate of the solid waste slurry is 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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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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