CN104492229A - Low-cost carbon dioxide capture system and method for pithead power plant - Google Patents
Low-cost carbon dioxide capture system and method for pithead power plant Download PDFInfo
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- CN104492229A CN104492229A CN201410822871.1A CN201410822871A CN104492229A CN 104492229 A CN104492229 A CN 104492229A CN 201410822871 A CN201410822871 A CN 201410822871A CN 104492229 A CN104492229 A CN 104492229A
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- magnetic valve
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 104
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 49
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 47
- 241000269793 Cryothenia peninsulae Species 0.000 title claims abstract description 15
- 238000000034 method Methods 0.000 title claims abstract description 13
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 84
- 230000003647 oxidation Effects 0.000 claims abstract description 78
- 238000009423 ventilation Methods 0.000 claims abstract description 65
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 32
- 238000011069 regeneration method Methods 0.000 claims abstract description 26
- 230000008929 regeneration Effects 0.000 claims abstract description 20
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 13
- 239000003546 flue gas Substances 0.000 claims abstract description 13
- 238000005065 mining Methods 0.000 claims abstract description 8
- 239000007789 gas Substances 0.000 claims description 60
- 230000001172 regenerating effect Effects 0.000 claims description 52
- 239000000919 ceramic Substances 0.000 claims description 30
- 238000010521 absorption reaction Methods 0.000 claims description 27
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 21
- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical compound NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 claims description 15
- 238000010438 heat treatment Methods 0.000 claims description 14
- 238000005265 energy consumption Methods 0.000 claims description 11
- 239000000446 fuel Substances 0.000 claims description 9
- 239000007788 liquid Substances 0.000 claims description 9
- 239000000779 smoke Substances 0.000 claims description 9
- 238000006243 chemical reaction Methods 0.000 claims description 7
- 238000000926 separation method Methods 0.000 claims description 6
- 238000009833 condensation Methods 0.000 claims description 3
- 230000005494 condensation Effects 0.000 claims description 3
- 238000001816 cooling Methods 0.000 claims description 3
- 238000006477 desulfuration reaction Methods 0.000 claims description 3
- 230000023556 desulfurization Effects 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims 1
- 239000005431 greenhouse gas Substances 0.000 abstract description 7
- 229960004424 carbon dioxide Drugs 0.000 description 40
- 235000011089 carbon dioxide Nutrition 0.000 description 8
- 238000007599 discharging Methods 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 4
- 238000011084 recovery Methods 0.000 description 3
- 239000003245 coal Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000006378 damage Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- ZZVUWRFHKOJYTH-UHFFFAOYSA-N diphenhydramine Chemical compound C=1C=CC=CC=1C(OCCN(C)C)C1=CC=CC=C1 ZZVUWRFHKOJYTH-UHFFFAOYSA-N 0.000 description 1
- 238000005553 drilling Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
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Abstract
The invention discloses a low-cost carbon dioxide capturing system and a low-cost carbon dioxide capturing method for a pithead power plant, wherein the system comprises a flue gas carbon dioxide capturing system and a ventilation air methane oxidation heat supply system, and heat generated by ventilation air methane oxidation is used for a regeneration heat supply system of the flue gas carbon dioxide capturing system of the pithead power plant through a ventilation air methane oxidation device; by effectively combining the carbon dioxide capture system and the ventilation air methane treatment system, the carbon dioxide capture cost is greatly reduced, and meanwhile, the emission reduction of methane greenhouse gas in a mining area and the energy utilization of ventilation air methane are realized.
Description
Technical field
The present invention relates to Technology of Reducing Greenhouse Gas Emissions field, be specifically related to pit-head power station low cost carbon dioxide capture system and method.
Background technology
A large amount of discharges of greenhouse gases are the one of the main reasons causing Global climate change.Carbon dioxide is one of main greenhouse gases, it to the contribution of Global Greenhouse Effect more than 60%.Coal-burning power plant is maximum CO2 emission source.Within the following long term, China will be all the general layout based on coal fired power generation.Therefore power-plant flue gas CO is carried out
2trapping is one of the most effective current reduction of greenhouse gas discharge approach.
Current, power plant's collecting carbonic anhydride is also in the engineering mimoir stage.The main cause of power-plant flue gas collecting carbonic anhydride technology large-scale promotion is hindered to be that trapping cost remains high.By current technical merit, hydramine method is adopted to carry out the unit trapping cost of power-plant flue gas collecting carbonic anhydride about 250-350 yuan/ton.Due to higher (the about 3.4GJ/ ton CO of carbon dioxide regeneration energy consumption
2), for CO
2the steam energy consumption cost of regeneration just accounts for the over half of totle drilling cost.Due to CO
2the required steam of trapping system generally derives from plant steam tube, and the later stage sets up large-scale CO
2trapping system can have influence on the regular supply of power plant's steam to the demand of steam, reduces power plants generating electricity efficiency.In addition, because power plant's steam comes from burning of coal heat supply, also power plant CO is just meaned
2the energy consumption of trapping system itself also result in the discharge of carbon dioxide.Here it is makes CO
2effective CER have a greatly reduced quality.
Visible, seek a kind of nearly zero cost, independent and clean carbon dioxide regeneration energy consumption source of supply, make CO
2trapping cost significantly reduces, and reduces the impact that carbon dioxide capture system causes power plant's heating demand simultaneously, and significantly promotes CO
2effective reduction of discharging equivalent of trapping system, is of great significance the large-scale promotion tool of power-plant flue gas collecting carbonic anhydride technology.
Summary of the invention
In order to overcome above-mentioned prior art Problems existing, the object of the present invention is to provide pit-head power station low cost carbon dioxide capture system and method, the factory site advantage special according to pit-head power station, introduce mine air-lack mash gas, by ventilation air methane oxidized apparatus, the heat that ventilation air gas oxidation produces is used for the breed-in system of pit-head power station carbon dioxide capture system.By effective combination of carbon dioxide capture system and ventilation air gas governing system, realize collecting carbonic anhydride cost and significantly reduce, realize the reduction of discharging of mining area methane greenhouse gases and the recovery energy of ventilation air gas simultaneously.
In order to realize foregoing invention object, the technical scheme that the present invention takes is:
Pit-head power station low cost carbon dioxide capture system, comprise smoke carbon dioxide capture system and ventilation air gas oxidation heating system, described smoke carbon dioxide capture system comprises demineralized water pretreater 1, by the absorption tower 3 that booster fan 2 is communicated with demineralized water pretreater 1, the bottom on described absorption tower 3 is communicated with regenerator 6 by rich solution pump 4 with lean solution/rich solution heat exchanger 5, described regenerator 6 top is communicated with knockout drum 7, the bottom of knockout drum 7 is communicated with regenerator 6 again by water pump, be communicated with the top on absorption tower 3 with lean solution/rich solution heat exchanger 5 by lean pump 8 bottom described regenerator 6, described regenerator 6 realizes the heat exchange of solution and steam in regenerator by reboiler 9, described ventilation air gas oxidation heating system comprises the flow-reversal control system 11 be communicated with the ventilation air gas from mining area ventilation shaft by blower fan 10, the regenerative oxidation device 12 be communicated with flow-reversal control system 11, described regenerative oxidation device 12 is communicated with the regenerator 6 of smoke carbon dioxide capture system by reboiler 9, carry out the heat exchange of solution and steam in regenerator, described regenerative oxidation device 12 carries out preheating by fuel burner nozzle 13 to it, described flow-reversal control system 11 is by the first magnetic valve A be connected in series successively, second magnetic valve B, 3rd magnetic valve C and the 4th magnetic valve D forms, described regenerative oxidation device 12 is made up of upper end thermal storage ceramic and lower end thermal storage ceramic, upper end thermal storage ceramic is connected between the first magnetic valve A and the second magnetic valve B, lower end thermal storage ceramic is connected between the 3rd magnetic valve C and the 4th magnetic valve D.
The capture method of pit-head power station low cost carbon dioxide capture system described above, power-plant flue gas sends into absorption tower 3 through booster fan 2, the CO in flue gas after carrying out desulfurization, dedusting by demineralized water pretreater 1
2absorbed by monoethanolamine MEA solution in absorption tower 3, remove CO
2after neat stress discharge from top, absorption tower 3; Absorb CO
2after ethanolamine solutions and rich solution flow into bottom absorption tower 3, be pressed into regenerator 6 through rich solution pump 4 and carry out CO
2regeneration; The CO that high temperature parses
2and part steam is discharged from regenerator 6 top, enters knockout drum 7 and carries out gas-liquid separation, thus obtain highly purified carbon dioxide after condensation; Isolated aqueous water is squeezed in regenerator 6 through water pump again; Parse CO
2after ethanolamine solutions and lean solution flow into bottom regenerator 6, be pressed in absorption tower 3 through lean pump 8, enter the circulation of next absorption/regeneration; Lean solution temperature after regeneration is higher, carries out preheating, can reduce rich solution regeneration energy consumption and lean solution cooling load by lean solution/rich solution heat exchanger 5 to the rich solution entering regenerator 6; CO in regenerator
2resolving is the endothermic reaction, and for maintaining solution temperature in regenerator, the regenerative oxidation device 12 being oxidized heating system by reboiler 9 and ventilation air gas is communicated with the heat exchange realizing solution and steam in regenerator;
From the ventilation air gas of mining area ventilation shaft through blower fan 10 and flow-reversal control system 11, enter regenerative oxidation device 12 and carry out thermal oxide, thus be CO by the methane oxidation in ventilation air gas
2and H
2o, and release heat; Due to the methane concentration < 0.75% of ventilation air gas, directly cannot burn, need the regenerative oxidation technique adopting flow-reversal to maintain reaction; Before ventilation air gas oxidation heating system starts, need to carry out preheating by fuel burner nozzle 13 pairs of regenerative oxidation devices 12, two sections of thermal storage ceramics are preheating to the thermal oxide light-off temperature 1000-1200 DEG C of ventilation air gas, then close preheating fuel burner nozzle 13, start blower fan 10 and introduce ventilation air gas; The the first magnetic valve A and the 3rd magnetic valve C that open flow-reversal control system 11 open, close the second magnetic valve B and the 4th magnetic valve D, ventilation air gas enters regenerative oxidation device 12 through the first magnetic valve A, absorb heat from regenerative oxidation device 12 upper end thermal storage ceramic and oxidation reaction occurs, the heat that oxidation produces is absorbed by regenerative oxidation device 12 lower end thermal storage ceramic, and tail gas is discharged through the 3rd magnetic valve C; When upper end thermal storage ceramic temperature is down to preset value, open the second magnetic valve B and the 4th magnetic valve D of flow-reversal control system 11, close the first magnetic valve A and the 3rd magnetic valve C, ventilation air gas enters regenerative oxidation device 12 through the 4th magnetic valve D, absorb heat from regenerative oxidation device 12 lower end thermal storage ceramic and oxidation reaction occurs, the heat that oxidation produces is absorbed by regenerative oxidation device 12 upper end thermal storage ceramic, and tail gas is discharged through the second magnetic valve B; Controlled by periodicity flow-reversal, the oxidation of ventilation air gas is continued to carry out; Flow to the length of switching cycle with ventilation air gas concentration, the design of flow and regenerative oxidation device 12 is relevant, and excessive cycle easily causes system to extinguish, and the cycle is too short, can reduce the efficiency of system;
Condensate liquid from regenerator 6 is introduced regenerative oxidation device 12 by water pump by reboiler 9 and is heated after gas-liquid separation, and the steam that regenerative oxidation device 12 generates enters reboiler 9 and carries out CO for solution in thermal regeneration tower 6
2regeneration.
In conventional power plants collecting carbonic anhydride technique, steam is generally taken from plant steam tube.In system of the present invention, steam comes from the heat recovery and utilization after ventilation air gas oxidation.Ventilation air gas is because calorific value is extremely low, the low-grade steam that heat recovery generally also can only provide less than 200 DEG C is carried out by oxidative system, purposes is limited, but the steam demand of carbon dioxide regeneration can be met, because the steam grade that carbon dioxide regeneration needs is not high, the general low-pressure steam that only need adopt about 130 DEG C.Compared to the prior art, tool has the following advantages in the present invention:
1) carbon dioxide regeneration energy consumption cost significantly reduces.Adopt conventional carbon dioxide trapping system, regenerate power plant's steam that carbon dioxide per ton need consume 3.4GJ, energy consumption cost is about 170 yuan.Adopt the described system of this invention, the energy consumption cost regenerating carbon dioxide per ton is no more than 10 yuan (mainly coming from the power consumption of weary wind blower fan).Therefore adopt this invention that regeneration energy consumption cost can be made to reduce by more than 90%.
2) actual reduction of greenhouse gas discharge equivalent promotes greatly.Adopt conventional carbon dioxide trapping system, because the supply of steam comes from coal-fired boiler in power plant, therefore also can bring new CO2 emission while capturing carbon dioxide.Trap the actual reduction of discharging equivalent of carbon dioxide per ton lower than 1 ton.After adopting the described system of this invention, the supply of steam comes from the oxidation (CH of methane in weary wind
4+ 2O
2→ CO
2+ 2H
2o).CH
4greenhouse effects are CO
221 times.By calculating, the methane trapping carbon dioxide per ton destruction is equivalent to the CO of reduction of discharging 2.3 tons of equivalents
2.Therefore, after adopting the described system of this invention, the actual reduction of discharging equivalent therefore trapping carbon dioxide per ton is about 3.3 tons.Therefore, actual reduction of discharging equivalent is more than 3 times of traditional trapping system.
Figure of description of the present invention is used to provide a further understanding of the present invention, forms a part of the present invention, and schematic description and description of the present invention, for explaining the present invention, does not form inappropriate limitation of the present invention.
Accompanying drawing explanation
Accompanying drawing is pit-head power station low cost carbon dioxide capture system schematic diagram of the present invention.
Detailed description of the invention
Below in conjunction with drawings and the specific embodiments, the present invention is described in further detail.
As shown in drawings, pit-head power station low cost carbon dioxide capture system of the present invention, comprise smoke carbon dioxide capture system and ventilation air gas oxidation heating system, described smoke carbon dioxide capture system comprises demineralized water pretreater 1, by the absorption tower 3 that booster fan 2 is communicated with demineralized water pretreater 1, the bottom on described absorption tower 3 is communicated with regenerator 6 by rich solution pump 4 with lean solution/rich solution heat exchanger 5, described regenerator 6 top is communicated with knockout drum 7, the bottom of knockout drum 7 is communicated with regenerator 6 again by water pump, be communicated with the top on absorption tower 3 with lean solution/rich solution heat exchanger 5 by lean pump 8 bottom described regenerator 6, described regenerator 6 realizes the heat exchange of solution and steam in regenerator by reboiler 9, described ventilation air gas oxidation heating system comprises the flow-reversal control system 11 be communicated with the ventilation air gas from mining area ventilation shaft by blower fan 10, the regenerative oxidation device 12 be communicated with flow-reversal control system 11, described regenerative oxidation device 12 is communicated with the regenerator 6 of smoke carbon dioxide capture system by reboiler 9, carry out the heat exchange of solution and steam in regenerator, described regenerative oxidation device 12 carries out preheating by fuel burner nozzle 13 to it, described flow-reversal control system 11 is by the first magnetic valve A be connected in series successively, second magnetic valve B, 3rd magnetic valve C and the 4th magnetic valve D forms, described regenerative oxidation device 12 is made up of upper end thermal storage ceramic and lower end thermal storage ceramic, upper end thermal storage ceramic is connected between the first magnetic valve A and the second magnetic valve B, lower end thermal storage ceramic is connected between the 3rd magnetic valve C and the 4th magnetic valve D.
As shown in drawings, the capture method of pit-head power station low cost carbon dioxide capture system of the present invention, power-plant flue gas sends into absorption tower 3 through booster fan 2, the CO in flue gas after carrying out desulfurization, dedusting by demineralized water pretreater 1
2absorbed by monoethanolamine MEA solution in absorption tower 3, remove CO
2after neat stress discharge from top, absorption tower 3; Absorb CO
2after ethanolamine solutions and rich solution flow into bottom absorption tower 3, be pressed into regenerator 6 through rich solution pump 4 and carry out CO
2regeneration; The CO that high temperature parses
2and part steam is discharged from regenerator 6 top, enters knockout drum 7 and carries out gas-liquid separation, thus obtain highly purified carbon dioxide after condensation; Isolated aqueous water is squeezed in regenerator 6 through water pump again; Parse CO
2after ethanolamine solutions and lean solution flow into bottom regenerator 6, be pressed in absorption tower 3 through lean pump 8, enter the circulation of next absorption/regeneration; Lean solution temperature after regeneration is higher, carries out preheating, can reduce rich solution regeneration energy consumption and lean solution cooling load by lean solution/rich solution heat exchanger 5 to the rich solution entering regenerator 6; CO in regenerator
2resolving is the endothermic reaction, and for maintaining solution temperature in regenerator, the regenerative oxidation device 12 being oxidized heating system by reboiler 9 and ventilation air gas is communicated with the heat exchange realizing solution and steam in regenerator;
From the ventilation air gas of mining area ventilation shaft through blower fan 10 and flow-reversal control system 11, enter regenerative oxidation device 12 and carry out thermal oxide, thus be CO by the methane oxidation in ventilation air gas
2and H
2o, and release heat; Due to the methane concentration of ventilation air gas very low (< 0.75%), directly cannot burn, need the regenerative oxidation technique adopting flow-reversal to maintain reaction; Before ventilation air gas oxidation heating system starts, need to carry out preheating by fuel burner nozzle 13 pairs of regenerative oxidation devices 12, two sections of thermal storage ceramics are preheating to the thermal oxide light-off temperature 1000-1200 DEG C of ventilation air gas, then close preheating fuel burner nozzle 13, start blower fan 10 and introduce ventilation air gas; The the first magnetic valve A and the 3rd magnetic valve C that open flow-reversal control system 11 open, close the second magnetic valve B and the 4th magnetic valve D, ventilation air gas is along solid arrow direction flowing in accompanying drawing: ventilation air gas enters regenerative oxidation device 12 through the first magnetic valve A, absorb heat from regenerative oxidation device 12 upper end thermal storage ceramic and oxidation reaction occurs, the heat that oxidation produces is absorbed by regenerative oxidation device 12 lower end thermal storage ceramic, and tail gas is discharged through the 3rd magnetic valve C; When upper end thermal storage ceramic temperature is down to preset value, open the second magnetic valve B and the 4th magnetic valve D of flow-reversal control system 11, close the first magnetic valve A and the 3rd magnetic valve C, ventilation air gas is along dotted arrow direction flowing in accompanying drawing: ventilation air gas enters regenerative oxidation device 12 through the 4th magnetic valve D, absorb heat from regenerative oxidation device 12 lower end thermal storage ceramic and oxidation reaction occurs, the heat that oxidation produces is absorbed by regenerative oxidation device 12 upper end thermal storage ceramic, and tail gas is discharged through the second magnetic valve B.Controlled by periodicity flow-reversal, the oxidation of ventilation air gas is continued to carry out.Flow to the length of switching cycle with ventilation air gas concentration, the design of flow and regenerative oxidation device 12 is relevant, and excessive cycle easily causes system to extinguish, and the cycle is too short, can reduce the efficiency of system.
Condensate liquid from regenerator 6 is introduced regenerative oxidation device 12 by water pump by reboiler 9 and is heated after gas-liquid separation, and the steam that regenerative oxidation device 12 generates enters reboiler 9 and carries out CO for solution in thermal regeneration tower 6
2regeneration.Suppose that ventilation air gas oxidator is adiabatic reactor, according to law of conservation of energy, following energy relationship can be obtained:
Steam enthalpy=ventilation air gas reaction heat (the weary wind enthalpy of exiting flue gas enthalpy import)
Because the concentration of ventilation air gas is unstable, generally fluctuate between 0.3-0.75%, therefore this system needs the stable heating by regulating the flow of ventilation air gas to maintain system.
Claims (2)
1. pit-head power station low cost carbon dioxide capture system, it is characterized in that: comprise smoke carbon dioxide capture system and ventilation air gas oxidation heating system, described smoke carbon dioxide capture system comprises demineralized water pretreater (1), by the absorption tower (3) that booster fan (2) is communicated with demineralized water pretreater (1), the bottom on described absorption tower (3) is communicated with regenerator (6) by rich solution pump (4) with lean solution/rich solution heat exchanger (5), described regenerator (6) top is communicated with knockout drum (7), the bottom of knockout drum (7) is communicated with regenerator (6) again by water pump, described regenerator (6) bottom is communicated with the top of absorption tower (3) with lean solution/rich solution heat exchanger (5) by lean pump (8), described regenerator (6) realizes the heat exchange of solution and steam in regenerator by reboiler (9), described ventilation air gas oxidation heating system comprises the flow-reversal control system (11) be communicated with the ventilation air gas from mining area ventilation shaft by blower fan (10), the regenerative oxidation device (12) be communicated with flow-reversal control system (11), described regenerative oxidation device (12) is communicated with the regenerator (6) of smoke carbon dioxide capture system by reboiler (9), carry out the heat exchange of solution and steam in regenerator, described regenerative oxidation device (12) carries out preheating by fuel burner nozzle (13) to it, described flow-reversal control system (11) is by the first magnetic valve (A) be connected in series successively, second magnetic valve (B), 3rd magnetic valve (C) and the 4th magnetic valve (D) composition, described regenerative oxidation device (12) is made up of upper end thermal storage ceramic and lower end thermal storage ceramic, upper end thermal storage ceramic is connected between the first magnetic valve (A) and the second magnetic valve (B), lower end thermal storage ceramic is connected between the 3rd magnetic valve (C) and the 4th magnetic valve (D).
2. the capture method of pit-head power station low cost carbon dioxide capture system described in claim 1, it is characterized in that: after power-plant flue gas carries out desulfurization, dedusting by demineralized water pretreater (1), absorption tower (3) is sent into, the CO in flue gas through booster fan (2)
2absorbed by monoethanolamine MEA solution in absorption tower (3), remove CO
2after neat stress discharge from absorption tower (3) top; Absorb CO
2after ethanolamine solutions and rich solution flow into absorption tower (3) bottom, through rich solution pump (4) press-in regenerator (6) carry out CO
2regeneration; The CO that high temperature parses
2and part steam is discharged from regenerator (6) top, enters knockout drum (7) and carries out gas-liquid separation, thus obtain highly purified carbon dioxide after condensation; Isolated aqueous water is squeezed in regenerator (6) through water pump again; Parse CO
2after ethanolamine solutions and lean solution flow into regenerator (6) bottom, in lean pump (8) press-in absorption tower (3), enter the circulation of next absorption/regeneration; Lean solution temperature after regeneration is higher, carries out preheating, can reduce rich solution regeneration energy consumption and lean solution cooling load by lean solution/rich solution heat exchanger (5) to the rich solution entering regenerator (6); CO in regenerator
2resolving is the endothermic reaction, and for maintaining solution temperature in regenerator, the regenerative oxidation device (12) being oxidized heating system by reboiler (9) and ventilation air gas is communicated with the heat exchange realizing solution and steam in regenerator;
From the ventilation air gas of mining area ventilation shaft through blower fan (10) and flow-reversal control system (11), enter regenerative oxidation device (12) and carry out thermal oxide, thus be CO by the methane oxidation in ventilation air gas
2and H
2o, and release heat; Due to the methane concentration < 0.75% of ventilation air gas, directly cannot burn, need the regenerative oxidation technique adopting flow-reversal to maintain reaction; Before ventilation air gas oxidation heating system starts, need to carry out preheating by fuel burner nozzle (13) to regenerative oxidation device (12), two sections of thermal storage ceramics are preheating to the thermal oxide light-off temperature 1000-1200 DEG C of ventilation air gas, then close preheating with fuel burner nozzle (13), start blower fan (10) and introduce ventilation air gas; The first magnetic valve (A) and the 3rd magnetic valve (C) of opening flow-reversal control system (11) are opened, close the second magnetic valve (B) and the 4th magnetic valve (D), ventilation air gas enters regenerative oxidation device (12) through the first magnetic valve (A), absorb heat from regenerative oxidation device (12) upper end thermal storage ceramic and oxidation reaction occurs, the heat that oxidation produces is absorbed by regenerative oxidation device (12) lower end thermal storage ceramic, and tail gas is discharged through the 3rd magnetic valve (C); When upper end thermal storage ceramic temperature is down to preset value, open the second magnetic valve (B) and the 4th magnetic valve (D) of flow-reversal control system (11), close the first magnetic valve (A) and the 3rd magnetic valve (C), ventilation air gas enters regenerative oxidation device (12) through the 4th magnetic valve (D), absorb heat from regenerative oxidation device (12) lower end thermal storage ceramic and oxidation reaction occurs, the heat that oxidation produces is absorbed by regenerative oxidation device (12) upper end thermal storage ceramic, and tail gas is discharged through the second magnetic valve (B); Controlled by periodicity flow-reversal, the oxidation of ventilation air gas is continued to carry out; Flow to the length of switching cycle with ventilation air gas concentration, the design of flow and regenerative oxidation device (12) is relevant, and excessive cycle easily causes system to extinguish, and the cycle is too short, can reduce the efficiency of system;
Condensate liquid from regenerator (6) is introduced regenerative oxidation device (12) by water pump by reboiler (9) and is heated after gas-liquid separation, and the steam that regenerative oxidation device (12) generates enters reboiler (9) and carries out CO for thermal regeneration tower (6) interior solution
2regeneration.
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| CN104857816A (en) * | 2015-04-29 | 2015-08-26 | 古浪鑫辉化工有限公司 | System and method for producing food grade carbon dioxide through lime kiln tail gases |
| CN108014603A (en) * | 2017-11-21 | 2018-05-11 | 华电电力科学研究院 | Crystallization ammonia process steam regeneration catches carbon system and method |
| CN109718636A (en) * | 2017-10-27 | 2019-05-07 | 株式会社东芝 | The method of operation of carbon dioxide separation recovery system and carbon dioxide separation recovery system |
| CN115282735A (en) * | 2022-10-09 | 2022-11-04 | 旭阳工程有限公司 | Carbon capture absorbent and absorption method and device |
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