CN220736979U - Carbon dioxide trapping and absorbing device suitable for flue gas discharged by natural gas boiler - Google Patents
Carbon dioxide trapping and absorbing device suitable for flue gas discharged by natural gas boiler Download PDFInfo
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- CN220736979U CN220736979U CN202320618122.1U CN202320618122U CN220736979U CN 220736979 U CN220736979 U CN 220736979U CN 202320618122 U CN202320618122 U CN 202320618122U CN 220736979 U CN220736979 U CN 220736979U
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 117
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 58
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 56
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 30
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 22
- 239000003546 flue gas Substances 0.000 title claims abstract description 22
- 239000003345 natural gas Substances 0.000 title claims abstract description 15
- 239000007788 liquid Substances 0.000 claims abstract description 62
- 238000010521 absorption reaction Methods 0.000 claims abstract description 41
- 230000008929 regeneration Effects 0.000 claims abstract description 25
- 238000011069 regeneration method Methods 0.000 claims abstract description 25
- 230000003009 desulfurizing effect Effects 0.000 claims abstract description 8
- 238000005406 washing Methods 0.000 claims abstract description 6
- 230000001172 regenerating effect Effects 0.000 claims abstract description 5
- 239000007789 gas Substances 0.000 claims description 30
- 238000007906 compression Methods 0.000 claims description 9
- 230000006835 compression Effects 0.000 claims description 8
- 238000001035 drying Methods 0.000 claims description 8
- 238000001179 sorption measurement Methods 0.000 claims description 8
- 238000005265 energy consumption Methods 0.000 abstract description 5
- 238000004064 recycling Methods 0.000 abstract description 3
- 229910002090 carbon oxide Inorganic materials 0.000 abstract 1
- 238000003795 desorption Methods 0.000 description 22
- 239000002250 absorbent Substances 0.000 description 12
- 230000002745 absorbent Effects 0.000 description 12
- 238000000034 method Methods 0.000 description 11
- 150000001412 amines Chemical class 0.000 description 10
- 239000012535 impurity Substances 0.000 description 9
- 239000002904 solvent Substances 0.000 description 9
- 238000002474 experimental method Methods 0.000 description 8
- 238000012360 testing method Methods 0.000 description 8
- 230000000694 effects Effects 0.000 description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 7
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 6
- 239000000047 product Substances 0.000 description 6
- 238000000746 purification Methods 0.000 description 6
- 239000002994 raw material Substances 0.000 description 6
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 5
- 150000001875 compounds Chemical class 0.000 description 5
- 238000001816 cooling Methods 0.000 description 5
- 238000009472 formulation Methods 0.000 description 5
- 239000000203 mixture Substances 0.000 description 5
- 229910052717 sulfur Inorganic materials 0.000 description 5
- 239000011593 sulfur Substances 0.000 description 5
- 239000002131 composite material Substances 0.000 description 4
- 238000005260 corrosion Methods 0.000 description 4
- 230000007797 corrosion Effects 0.000 description 4
- 238000001704 evaporation Methods 0.000 description 4
- 239000002808 molecular sieve Substances 0.000 description 4
- 230000002829 reductive effect Effects 0.000 description 4
- 238000011160 research Methods 0.000 description 4
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 4
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 3
- 238000004458 analytical method Methods 0.000 description 3
- 230000008020 evaporation Effects 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 238000009835 boiling Methods 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 238000002144 chemical decomposition reaction Methods 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000004891 communication Methods 0.000 description 2
- 230000003247 decreasing effect Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 230000036961 partial effect Effects 0.000 description 2
- 239000003755 preservative agent Substances 0.000 description 2
- 230000002335 preservative effect Effects 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- KXDHJXZQYSOELW-UHFFFAOYSA-M Carbamate Chemical compound NC([O-])=O KXDHJXZQYSOELW-UHFFFAOYSA-M 0.000 description 1
- 229910002651 NO3 Inorganic materials 0.000 description 1
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 1
- 239000006096 absorbing agent Substances 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 239000003463 adsorbent Substances 0.000 description 1
- 239000003963 antioxidant agent Substances 0.000 description 1
- 230000003078 antioxidant effect Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- -1 compound amine Chemical class 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 238000005261 decarburization Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 239000007857 degradation product Substances 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000005461 lubrication Methods 0.000 description 1
- 238000010587 phase diagram Methods 0.000 description 1
- 239000003507 refrigerant Substances 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
- 230000036962 time dependent Effects 0.000 description 1
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- Treating Waste Gases (AREA)
Abstract
The utility model belongs to the field of carbon oxide recycling, and in particular relates to a carbon dioxide trapping and absorbing device suitable for flue gas discharged by a natural gas boiler, which comprises a desulfurizing device, an alkaline washing tower, an absorbing tower and a regenerating tower which are sequentially communicated; the front end of the desulfurizing device is communicated with the flue; the rich liquid outlet of the absorption tower is communicated with the liquid inlet of the regeneration tower through a first pipeline; the liquid outlet of the regeneration tower is communicated with the lean liquid inlet of the absorption tower through a second pipeline; the first pipeline and the second pipeline exchange heat through a lean-rich liquid heat exchanger; the air outlet of the regeneration tower is communicated with the gas-liquid separator. The device of the utility model reduces the absorption energy consumption by heat exchange.
Description
Technical Field
The utility model relates to the field of carbon dioxide resource utilization, in particular to a carbon dioxide capturing and absorbing device suitable for flue gas discharged by a natural gas boiler.
Background
The description of the background art to which the present utility model pertains is merely for illustrating and facilitating understanding of the summary of the utility model, and should not be construed as an explicit recognition or presumption by the applicant that the applicant regards the prior art as the filing date of the first filed application.
The capturing and recycling treatment of carbon dioxide in flue gas is always a focus of social attention, however, the current absorption of carbon dioxide lacks a treatment device and a treatment process of a system, and the problems of high energy consumption and poor absorption effect can occur in the absorption and analysis processes of carbon dioxide.
Disclosure of Invention
The embodiment of the utility model aims to provide a carbon dioxide capturing and absorbing device suitable for flue gas discharged by a natural gas boiler, and the device reduces energy consumption for absorbing through heat exchange.
The aim of the embodiment of the utility model is realized by the following technical scheme:
the carbon dioxide trapping and absorbing device suitable for the flue gas discharged by the natural gas boiler comprises a desulfurizing device, an alkaline washing tower, an absorbing tower and a regenerating tower which are communicated in sequence; the front end of the desulfurizing device is communicated with the flue;
the rich liquid outlet of the absorption tower is communicated with the liquid inlet of the regeneration tower through a first pipeline; the liquid outlet of the regeneration tower is communicated with the lean liquid inlet of the absorption tower through a second pipeline; the first pipeline and the second pipeline exchange heat through a lean-rich liquid heat exchanger; the air outlet of the regeneration tower is communicated with the gas-liquid separator.
Further, a gas outlet is arranged on the absorption tower and is communicated with the flue.
Further, a lean solution cooler is arranged on the second pipeline.
Further, the device also comprises a solution reboiler, wherein the solution reboiler is communicated with the regeneration tower through a circulating pipeline.
Further, the device also comprises a carbon dioxide treatment device, and the carbon dioxide treatment device is communicated with the air outlet of the gas-liquid separator.
Further, the carbon dioxide treatment device comprises a precooling device, a compression device, an adsorption device, a drying device, a condensing device and a purifying device which are sequentially communicated.
Further, the liquid outlet of the gas-liquid separator is communicated with the regeneration tower.
The embodiment of the utility model has the following beneficial effects:
the rich liquid is fed from the upper part and the middle part of the regeneration tower, and partial CO is desorbed by stripping 2 Then enter a reboiler to make CO therein 2 Further desorbing. Desorption of CO 2 The lean solution (105 ℃) flows out from the bottom of the regeneration tower, part of steam is flashed out by a flash tank and is pressurized and recycled back to the desorption tower to recycle heat; the heat of the lean liquid flowing out of the flash tank is recovered by the lean-rich liquid heat exchanger, then the temperature is reduced to 60 ℃, the lean liquid is pumped to a lean liquid cooler, and the lean liquid is cooled to 40 ℃ and then enters the absorption tower. The solvent is circulated back and forth to form continuous absorption and desorption of CO 2 CO 2 The trapping rate of the catalyst is more than 90 percent.
The air source of the compression and rectification purification unit is derived from CO2 regenerated gas of the CO2 trapping device, wherein main impurities are sulfur-containing substances and other trace impurities, and the main impurities are adsorbed and removed in an adsorber through high-quality activated carbon, so that the product index is fundamentally ensured to meet the food-grade quality standard, no large amount of waste water and waste liquid are discharged in the production process, no harmful substances are contained in discharged tail gas, and the discharge requirement is completely met.
Drawings
FIG. 1 is a schematic flow chart of the trapping process according to the utility model.
Detailed Description
The present application is further described below with reference to examples.
In order to more clearly describe embodiments of the present utility model or technical solutions in the prior art, in the following description, different "an embodiment" or "an embodiment" does not necessarily refer to the same embodiment. Various embodiments may be substituted or combined, and other implementations may be obtained from these embodiments by those of ordinary skill in the art without undue burden.
Referring to fig. 1, a carbon dioxide capturing and absorbing device suitable for flue gas discharged by a natural gas boiler comprises a desulfurizing device, an alkaline washing tower 1, an absorbing tower 2 and a regenerating tower 3 which are sequentially communicated; the front end of the desulfurizing device is communicated with the flue; (an induced draft fan 4 is adopted between the alkaline washing tower 1 and the absorption tower 2 to send the flue gas into the absorption tower 2);
the rich liquid outlet of the absorption tower 2 is communicated with the liquid inlet of the regeneration tower 3 through a first pipeline; the liquid outlet of the regeneration tower 3 is communicated with the lean liquid inlet of the absorption tower 2 through a second pipeline; the first pipeline and the second pipeline exchange heat through a lean rich liquid heat exchanger 6; the air outlet of the regeneration tower 3 is communicated with a gas-liquid separator 9.
In some embodiments of the present utility model, the absorber 2 is provided with a gas outlet, and the gas outlet is communicated with the flue.
In some embodiments of the utility model, the second pipe is provided with a lean liquor cooler 7.
In some embodiments of the present utility model, a solution reboiler 10 is further included, and the solution reboiler 10 is in communication with the regeneration tower 3 through a circulation pipeline.
In some embodiments of the present utility model, the apparatus further comprises a carbon dioxide treatment device, and the carbon dioxide treatment device is communicated with the air outlet of the gas-liquid separator 9.
In some embodiments of the present utility model, the carbon dioxide treatment device includes a pre-cooling device, a compression device, an adsorption device, a drying device, a condensing device, and a purifying device, which are sequentially connected.
In some embodiments of the present utility model, the liquid outlet of the gas-liquid separator 9 is in communication with the regeneration tower 3.
In order to improve the absorption effect, the applicant independently develops a carbon dioxide trapping absorbent suitable for the flue gas discharged by the natural gas boiler, and designs a carbon dioxide trapping process flow of the gas boiler on the basis.
The applicant has carried out a number of studies to obtain the effect of the absorbent: the optimal concentration ratio of the MEA-DETA solution is 5:5, the optimal concentration ratio of the MEA-TETA compound solution is 6:4, the optimal concentration ratio of the MEA-TEPA compound solution is 6:4, and the optimal concentration ratio of the MEA-PEHA compound solution is 5:5. Comparing the absorption and desorption properties of the four compound solutions to obtain the optimal solvent formula.
Analysis of each curve can show that the absorption rate of the MEA-PEHA solution is significantly higher than the other three curves, and the absorption rate of the MEA-DETA solution is the lowest. The carbon dioxide absorption capacity of the four solutions is sequentially MEA-PEHA solution > MEA-TEPA solution > MEA-TETA solution > MEA-DETA solution.
From the graph, the absorption rate change curve of the MEA-PEHA solution is obviously higher than that of other curves, and the change rule is consistent with the change rule of the absorption amount with time.
As described above, the time-dependent curves of the desorption rates of the four formulation solvents show high coincidence, and the change rule is that the desorption rates of the four formulation solvents are rapidly increased and then gradually decreased at the initial stage of the test, and the desorption rates of the four formulation solvents are basically consistent.
The desorption rate of the MEA-DETA solution is highest and the desorption rate of the MEA-PEHA solution is lowest.
The results of the four formulation solvent desorption experiments are shown in Table 1. As can be seen from the table, the MEA-PEHA solution has a minimum desorption temperature of 68℃and a minimum constant boiling temperature of 102 ℃.
TABLE 1 Desorption experiment results for different absorbent solutions
According to the test results, the absorption effect, the desorption effect and the desorption energy consumption of each solution are combined, and when the concentration ratio of the MEA-PEHA compound solution is 5:5, the test effect is optimal. Therefore, the optimal binary compound solvent under the test conditions is MEA-PEHA solution with the concentration ratio of 5:5.
Sulfur and nitrate resistance analysis of composite solutions
SO in flue gas 2 Research on influence on trapping performance
Test conditions: feed gas SO 2 ～1000ppm，CO 2 About 12 percent of raw material gas about 3.5Nm 3 /h。
TABLE 2 Desorption experiment results for different absorbent solutions
Complex amine solution vs SO 2 The absorptivity of (c) is close to 100%. As the total sulfur content in the solution increases, CO 2 The absorption rate decreases. SO in regenerated gas 2 The content was always less than 1ppm, indicating SO 2 It is difficult to regenerate under the test conditions.
NO in flue gas x Research on influence on trapping performance
Test conditions: feed gas CO 2 About 12 percent of raw material gas about 3.5Nm 3 /h。
TABLE 3 Desorption experiment results for different absorbent solutions
To verify NO x The influence of accumulation in the solvent on carbon absorption is carried out to carry out a high-concentration nitrogen oxide enhanced absorption test to study the influence on CO 2 Influence of absorption properties.
TABLE 4 Desorption experiment results for different absorbent solutions
By CO 2 The trapped pilot experiment study can lead to the following conclusions:
whether the single-component absorbent solution or the binary compound absorbent solution, the absorption capacity can be rapidly increased at the initial stage of the experiment, then the increase amplitude is gradually reduced, and the absorption rate and the desorption rate both show a change rule of increasing first and then decreasing.
The best concentration ratio of each group of binary compound absorbent solution can be obtained by combining the results of absorption and desorption experiments: the optimal concentration ratio of the MEA-DETA solution is 5:5, the optimal concentration ratio of the MEA-TETA compound solution is 6:4, the optimal concentration ratio of the MEA-TEPA compound solution is 6:4, and the optimal concentration ratio of the MEA-PEHA compound solution is 5:5.
From the experimental effect only, comparing the four binary compound absorbent solutions results in an MEA-PEHA solution with an optimal formulation of 5:5 concentration ratio.
The main reason why the organic amine method causes serious equipment corrosion is that the organic amine and CO 2 The carbamate and the chemical degradation products of the organic amine produced by the reaction. A great deal of research is carried out at home and abroad, and although a certain progress is made in the aspect of preservative development, the problem of reducing equipment corrosion caused by reducing organic amine degradation is not thoroughly solved. Through a great deal of experimental research, firstly, antioxidant and active amine are added to solve the chemical degradation of organic amine, and a group of preservative is developed on the basis of the absorption system and is mixed into the compound amine solution, so that the corrosion rate of the solution to equipment is smaller than that of the solution0.076mm/a, and fundamentally solves the technical problem of serious corrosion of the organic amine method to equipment.
Summary of the process
Flue gas (65 ℃ and normal pressure) from the outlet of the desulfurization absorption tower 2 is subjected to alkaline washing pretreatment and then cooled to 40 ℃, and enters a capturing and purifying device for decarburization treatment. Absorbing CO in flue gas by adopting organic amine composite absorbent 2 The flue gas enters the absorption tower 2 from the bottom of the tower and reversely contacts with the absorption liquid, and the interstage cooling technology is utilized to reduce the reaction heat, improve the absorption efficiency and absorb CO 2 The rich liquid is sent to a lean-rich liquid heat exchanger 6 from the bottom of the tower through a pump 5, and is sent to the regeneration tower 3 after heat is recovered. De-aspirating CO 2 Separating with water vapor to remove water to obtain product CO with purity of 99.5% (dry basis) or more 2 And (5) entering a subsequent compression process. Condensed water condensed and separated from the regenerated gas is returned to the underground tank, and a liquid supplementing pump is adopted to regularly supplement liquid for the regeneration tower 3.
The rich liquid is fed from the upper part and the middle part of the regeneration tower 3, and partial CO is desorbed by stripping 2 Then enters a reboiler 10 to make CO therein 2 Further desorbing. Desorption of CO 2 The lean solution (105 ℃) flows out from the bottom of the regeneration tower 3, and part of steam is flashed out by a flash tank to be pressurized and recovered to the desorption tower to recover heat; the heat of the lean liquid flowing out of the flash tank is recovered by the lean-rich liquid heat exchanger 6, then the temperature is reduced to 60 ℃, the lean liquid is sent to the lean liquid cooler 7 by the pump 8, and the lean liquid is cooled to 40 ℃ and then enters the absorption tower 2. The solvent is circulated back and forth to form continuous absorption and desorption of CO 2 CO 2 The trapping rate of the catalyst is more than 90 percent.
The regeneration energy consumption of 30wt% composite amine absorbent is less than or equal to 3.0GJ/t CO 2 The cyclic absorption load is more than or equal to 23LCO 2 solution/L.
The air source of the compression and rectification purification unit is derived from CO 2 Trapping device CO 2 The regenerated gas contains sulfur and other trace impurities as main impurities, and is mainly adsorbed and removed in an adsorber through high-quality activated carbon, so that the product index is basically ensured to meet the food-grade quality standard, no large amount of waste water and waste liquid are discharged in the production process, the discharged tail gas basically contains no harmful substances, and the discharge is completely satisfiedRequirements.
The project adopts the combined technology of precooling, adsorption, drying and low-temperature rectification.
(1) Precooling: the precooler is used for reducing the temperature of the carbon dioxide to ensure that the outlet temperature is about 15 ℃.
(2) Compression: the device adopts a medium pressure method to produce liquid carbon dioxide, and according to the thermodynamic condition of a carbon dioxide phase diagram, pure carbon dioxide can obtain liquid carbon dioxide as long as the condition of a carbon dioxide liquefying region with the pressure of 2.1MPa and the temperature of minus 20 ℃ can be kept. Because the purity of the raw material gas carbon dioxide entering the device is more than 99% (dry basis), and the rest is non-condensable gas, in order to reduce the carbon dioxide loss in the purification process, the final pressure of the raw material gas carbon dioxide is required to be increased to 2.5MPa through three-stage compression without oil lubrication, R22 is used for evaporation at the temperature of minus 28 ℃ to minus 31 ℃, and the compressed carbon dioxide gas is indirectly cooled to minus 25 ℃ to be liquefied.
(3) Adsorption: the adsorber is filled with active carbon to adsorb sulfur-containing impurities contained in the raw material gas and possibly oil-containing impurities brought by the compressor.
(4) And (3) drying: the molecular sieve is filled in the dryer, mainly for satisfying the following conditions: (1) the quality index that the water content of the liquid carbon dioxide product is less than or equal to 20ppm is satisfied; (2) in order to ensure that the saturated moisture in the carbon dioxide gas source is frozen at low temperature to block the pipeline and equipment in the process of liquefying and purifying the carbon dioxide, so that the production cannot be continued; and (3) removing trace water in the gas by utilizing the adsorption of the molecular sieve adsorbent to water, so as to ensure that the moisture of the carbon dioxide raw material gas after precooling and drying is less than or equal to 20ppm. And (3) heating and regenerating the molecular sieve after adsorption saturation, and recycling the molecular sieve. The drying tower adopts a one-open one-standby mode.
(5) Condensing and liquefying: the discharged gas containing 99% of carbon dioxide is subjected to the purification procedures of compression, precooling, adsorption, drying and the like, and then enters a condenser for condensation and liquefaction. Evaporating the liquid R22 at-25 to-30 ℃, and indirectly cooling the compressed carbon dioxide gas to condense and liquefy the carbon dioxide gas into liquid carbon dioxide.
(6) Purifying: the liquefied liquid carbon dioxide is purified, a composite rectification purification tower is adopted, and impurities are separated under specific conditions by utilizing a low-temperature rectification principle according to the difference of boiling points of the carbon dioxide and impurity components, so that the purity of the carbon dioxide is improved, a qualified liquid carbon dioxide product is obtained, and the gas consumption of the product is reduced.
(7) Auxiliary facilities:
r507 condensing system: the process device adopts a medium pressure method to produce liquid carbon dioxide. And cooling and liquefying carbon dioxide gas, and cooling discharged air at the top of the purification tower through a refrigerating unit. R507 is taken as a refrigerant, cold energy is transferred to carbon dioxide to liquefy the carbon dioxide through low-temperature evaporation of the R507, then the gaseous R507 is compressed by an ice machine and condensed by an evaporation condenser, the gaseous R507 is condensed into liquid R507, and then the liquid R507 is evaporated by the condenser to absorb heat, thus completing the refrigeration cycle.
It should be noted that the above embodiments can be freely combined as needed. The above description is only of the preferred embodiments of the present utility model and is not intended to limit the present utility model, but various modifications and variations can be made to the present utility model by those skilled in the art. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present utility model should be included in the protection scope of the present utility model.
Claims (7)
1. The carbon dioxide trapping and absorbing device suitable for the flue gas discharged by the natural gas boiler is characterized by comprising a desulfurizing device, an alkaline washing tower, an absorbing tower and a regenerating tower which are sequentially communicated; the front end of the desulfurizing device is communicated with the flue;
the rich liquid outlet of the absorption tower is communicated with the liquid inlet of the regeneration tower through a first pipeline; the liquid outlet of the regeneration tower is communicated with the lean liquid inlet of the absorption tower through a second pipeline; the first pipeline and the second pipeline exchange heat through a lean-rich liquid heat exchanger; the air outlet of the regeneration tower is communicated with the gas-liquid separator.
2. The carbon dioxide capturing and absorbing device suitable for flue gas discharged by a natural gas boiler according to claim 1, wherein a gas outlet is arranged on the absorbing tower, and the gas outlet is communicated with a flue.
3. The carbon dioxide capturing and absorbing device suitable for flue gas discharged from a natural gas boiler according to claim 2, wherein the second pipeline is provided with a lean solution cooler.
4. The carbon dioxide capture and absorption device suitable for flue gas discharged from a natural gas boiler according to claim 2, further comprising a solution reboiler, wherein the solution reboiler is communicated with the regeneration tower through a circulation pipeline.
5. The carbon dioxide capturing and absorbing device suitable for flue gas discharged from a natural gas boiler according to claim 2, further comprising a carbon dioxide treatment device, wherein the carbon dioxide treatment device is communicated with the gas outlet of the gas-liquid separator.
6. The carbon dioxide capturing and absorbing device suitable for flue gas discharged from a natural gas boiler according to claim 5, wherein the carbon dioxide treatment device comprises a precooling device, a compression device, an adsorption device, a drying device, a condensing device and a purifying device which are sequentially communicated.
7. The carbon dioxide capturing and absorbing device suitable for flue gas discharged by a natural gas boiler according to claim 2, wherein the liquid outlet of the gas-liquid separator is communicated with the regeneration tower.
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| CN202320618122.1U CN220736979U (en) | 2023-03-27 | 2023-03-27 | Carbon dioxide trapping and absorbing device suitable for flue gas discharged by natural gas boiler |
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| CN202320618122.1U CN220736979U (en) | 2023-03-27 | 2023-03-27 | Carbon dioxide trapping and absorbing device suitable for flue gas discharged by natural gas boiler |
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| CN116422105A (en) * | 2023-03-27 | 2023-07-14 | 北京市燃气集团有限责任公司 | Carbon dioxide capturing and absorbing method suitable for flue gas discharged by natural gas boiler |
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| CN116422105A (en) * | 2023-03-27 | 2023-07-14 | 北京市燃气集团有限责任公司 | Carbon dioxide capturing and absorbing method suitable for flue gas discharged by natural gas boiler |
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