CN204522740U - A kind of fluidized system of direct trapping mineralising carbon dioxide in flue gas - Google Patents
A kind of fluidized system of direct trapping mineralising carbon dioxide in flue gas Download PDFInfo
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- CN204522740U CN204522740U CN201520151601.2U CN201520151601U CN204522740U CN 204522740 U CN204522740 U CN 204522740U CN 201520151601 U CN201520151601 U CN 201520151601U CN 204522740 U CN204522740 U CN 204522740U
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Abstract
A kind of fluidized system of direct trapping mineralising carbon dioxide in flue gas, comprise: pretreatment unit, comprising the dry powder mill for grinding and/or for heat add thermal incinerator and/or for the stirred autoclave of alkaline process desiliconization, filter press and rotary drum drier; Flue-gas temperature humidity adjustment unit, is arranged in the bypass of flue, comprises the bubble tower that liquid is housed, and the flue gas going out bypass enters bubble tower and realizes temperature and humidity regulation; Fluidized-bed reactor, picks out the solid material of pretreatment unit and goes out the flue gas of flue-gas temperature humidity adjustment unit; Cyclone separator, the dusty gas picking out fluidized-bed reactor realizes gas solid separation, wherein gained gas is delivered to flue and is discharged from chimney, the utility model system processing power is large, and size is little, takes up an area few, be convenient to continued operation, convenient to be combined with power plant existing system, while flyash after decarburization do not affect the original use approach of fly ash in electric power plant, there is lower decarburization cost.
Description
Technical field
The utility model relates to smoke carbon dioxide capture and utilizes technical field, particularly a kind of fluidized system of direct trapping mineralising carbon dioxide in flue gas.
Background technology
Atmospheric greenhouse gas concentration raises the Global Greenhouse Effect caused, and causes iceberg thawing, sea level rise, species reduce, the multiple climate damage in all parts of the world takes place frequently, bring serious financial consequences and threaten human survival.Carbon dioxide (CO
2) distribute as the overall control in topmost greenhouse gases its futures and Emission Right the emphasis having become international climate negotiation.National governments and energy enterprise more and more pay attention to CO
2the research of emission control technique, some countries have taken the lead in starting substantial decarburization work.Along with China's carbon emission amount exceedes the reinforcement of the U.S. and the international cry reduced discharging, the Chinese government made promise in 2009 to the world and reduces 40-45% to the year two thousand twenty per GDP carbon emission amount.The resource general layout of China's " rich coal, few oil, has gas " determines the main body that coal is China's energy supply, and in China's primary energy, coal fired power generation proportion is close to 65%, so CO
2discharge is main from coal-burning power plant, accounts for the 40-50% of total discharge.Power plant's collecting carbonic anhydride and Plugging Technology Applied must become the medium-term and long-term technical need of China's low carbon development strategy.
CO
2mineralising is sealed up for safekeeping by CO
2react under certain condition with the alkaline-earth metal in ore or solid waste and produce carbonate to realize the technology of solid carbon.This technology can realize CO
2forever seal up for safekeeping, environmental risks is little, and mineral resources can be utilized wide, and ability of sealing up for safekeeping is strong, is the very potential Technology of Reducing Greenhouse Gas Emissions of one.But, due to the CO developed at present
2there is long flow path in mineralization process, reaction rate is low, equipment size is large, severe reaction conditions, energy consumption are high, chemical reagent reclaims difficulty, produces the shortcomings such as secondary pollution, and the applicable ore such as serpentine, olivine making mineralising raw material of external main research has handicraft to process raw material at China Chang Zuowei, causes cost of material high.These all hamper CO
2mineralising Plugging Technology Applied is in the commercialization process of China.
On the other hand, the annual emissions of China's coal-burning power plant's flyash has reached 100,000,000 tons, some flyash calcium oxide (CaO) content higher (mass fraction can reach more than 20%), is suitable for very much mineralising and seals CO in coal-fired flue-gas up for safekeeping
2.In addition, the solid waste also having a large amount of calcium carbide, cement and iron and steel enterprise to produce, is also rich in CaO, also can be used as the raw material of mineralising.So, can suit measures to local conditions to select solid waste as CO in China
2the raw material that mineralising is sealed up for safekeeping.
Summary of the invention
In order to overcome the shortcoming of above-mentioned prior art, the purpose of this utility model is the fluidized system providing a kind of direct trapping mineralising carbon dioxide in flue gas, utilize high calcium discarded object (flyash, carbide slag, slag, waste and old cement) to be raw material, adopt gas-solid mutually directly react fluidized-bed process trapping and mineralising flue gas in CO
2, effectively can improve the utilization of flyash and can CO be reduced
2discharge is a kind of Novel greenhouse gas abatement technology being applicable to very much China's national situation.
To achieve these goals, the technical solution adopted in the utility model is:
A fluidized system for direct trapping mineralising carbon dioxide in flue gas, comprising:
Pretreatment unit 7, comprise dry powder mill for grinding and/or for heat add thermal incinerator and/or for the stirred autoclave of alkaline process desiliconization, filter press and rotary drum drier;
Flue-gas temperature humidity adjustment unit 9, is arranged in the bypass of flue, comprises the bubble tower 15 that liquid is housed, and the flue gas going out bypass enters bubble tower 15 and realizes temperature and humidity regulation;
Fluidized-bed reactor 10, picks out the solid material of pretreatment unit 7 and goes out the flue gas of flue-gas temperature humidity adjustment unit 9;
Cyclone separator 11, the dusty gas picking out fluidized-bed reactor 10 realizes gas solid separation, and wherein gained gas is delivered to flue and discharged from chimney 13.
The outlet conduit of described bubble tower 15 arranges attemperator.
Described flue is disposed with SCR reactor 5, electrostatic precipitator 6 and FGD absorption tower 8 along flow of flue gas direction, described electrostatic precipitator 6 gained dust delivers to pretreatment unit 7 as solid material, electrostatic precipitator 6 gained flue gas enters FGD absorption tower 8 and carries out desulfurization, described bypass is arranged on the flue after desulfurization, compressor 14 is provided with, before compressor 14 is arranged at bubble tower 15 in bypass.
A part for the solid product of described cyclone separator 11 is recycled to fluidized-bed reactor 10 and recycles.
The following technique of device support of the present utility model:
The first step, collects high calcium discarded object and grinds stand-by;
Second step, fume emission flue is opened bypass and draws one flue gas and regulate temperature and humidity through temperature and humidity regulator, temperature regulating range is 40-90 DEG C, and the adjustable range of humidity is 5-60% (relative humidity);
3rd step, in a fluidized bed reactor by the flue gas after temperature and humidity regulation and described high calcium discarded object and to haptoreaction;
4th step, the dusty gas feeding cyclone separator going out fluidized-bed reactor after reaction carries out gas solid separation, and gained gas is sent former fume emission flue back to and entered smoke stack emission.
Wherein, described high calcium discarded object can be flyash, carbide slag, slag or waste and old cement etc., and General Requirements wherein CaO mass fraction is more than 20%, and granularity is 20-80 micron, has good chemical reactivity.Therefore, see whether need flyash to carry out pretreatment, preprocess method mainly contains three kinds: fine gtinding depending on concrete condition, heat treatment and alkaline process desiliconization process.Preprocess method can select one or more to use according to the concrete condition of raw material simultaneously, to reach the requirement of direct mineralising fluidized-bed process.Judge that raw material has grain graininess, crystal phase structure and CaO content 3 point the need of pretreated standard.Get after ash sample analyzes, adopt different pretreatments method targetedly in light of the circumstances.
Flue gas is power-plant flue gas, high calcium discarded object be power-plant flue gas electrostatic precipitation after gained flyash time, achieve the trapping of fly ash in electric power plant to self carbon dioxide in flue gas.
Such as, when selecting flyash, carry out following analyzing and processing:
(1) whether there is the granularity of 30-80 micron, generally, the granularity of flyash is at 40 microns, this granularity is just in time applicable to the minimum fluidization velocity needed for fluid bed, grinding can be pulverized again, but the glassy phase crystal structure that sometimes fine gtinding can be adopted to destroy flyash in order to improve reactivity further creates more lattice defects, and after further fine gtinding, granularity is reduced to 20 microns.
(2) crystalline phase in flyash is mainly based on corundum-mullite and glassy phase, and structure is comparatively fine and close, and surface-active is not high.This mainly because flyash is that cooling is formed caused by the crystal of bead shape fast in flue, can adopt high-temperature heat treatment under 600 degree within 2 hours, to destroy the crystal structure of bead surface to improve its chemical reactivity.
(3) whether CaO content needs to reach more than 20%, and such as C level flyash can not do pretreatment, and F level flyash need do alkaline process desiliconization process, general NaOH or NaCO adopting 0.5-2mol/l
3solution by solid-to-liquid ratio 100-250g/l by flyash hydro-thermal reaction 3 hours under 100 degree, reacted mortar filtration drying both the flyash after desiliconization, and filtrate can put forward aluminium use containing sodium metaaluminate and sodium metasilicate height.
Described bypass is opened on the flue after desulfurization, can certainly open before desulfurization, and TV structure space determines.Humidistat can use the form of two platen press bubble tower, first flue gas is carried out water saturation, then controls the pressure that exports, regulates flue gas from taking moisture in tower by changing pressure.The flue gas of flue is generally negative pressure (-40kPa), needs first through a compressor, pressure is elevated to pressure-fired (200kPa), then the outlet pressure controlling bubble tower regulates and takes moisture.Note will being incubated to keep moisture stable from the flue gas duct after bubble tower.
The minimum fluidization velocity of fluidized-bed reactor entrance calculates according to fly ash grain, generally need at more than 0.004m/s, initial bubbling rate calculates according to fly ash grain, generally need at more than 0.012m/s, consider resistance degradation factor in a practical situation, selection air velocity is 0.1-0.5m/s, and in reactor, the charge ratio of solid and gas row (grey gas than) remain on 5-15kg flyash/m to flyash at 3-20min the time of staying
3flue gas, depending on CO in CaO content and flue gas
2concentration and determining.Because flue gas has certain humidity can form one deck liquid film in flyash fixed surface, the CaO in the surface of solids and duct can be solved Ca by the water power in liquid film
+, and liquid film also can absorb the CO in flue gas simultaneously
2and ionize out HCO
3 -and CO
3 2-, (60-90 degree Celsius) Ca at a certain temperature
+and HCO
3 -or CO
3 2-reaction generates calcium carbonate fast.Through fluidized-bed reactor dusty gas out through cyclone separator, gas is discharged from top, and lower end becomes the flyash containing calcium carbonate of large (can increase to 100 microns) for particle diameter after reaction.Get gaseous sample in the place of flue gas turnover fluidized system and survey wherein CO through flue gas analyzer
2and SO
2content.Find CO
29% is reduced to from about 13% concentration of entrance, and SO
2concentration is from 100mg/Nm
3be reduced to 35mg/Nm
3.
Cyclone separator top decarburization gas is out got back to former flue collector and is entered smoke stack emission, and some flyash can reenter fluid bed and continue reaction, and collective low to separating solids product section be back to fluidized-bed reactor and recycle., reflux ratio controls between 1:1-5:1.Solid product can be used to powder process coal ash cement, or as uses such as ground based fillers.
Compared with prior art, the beneficial effects of the utility model are:
1, system architecture is simple, only comprises pretreatment (as cancelled for C level high-calcium fly ass), warm and humid adjustment and fluid bed and piece-rate system.
2, avoid a large amount of high pressure slurry reactor stills used in traditional mineralising, adopt fluidized-bed reactor to be convenient to continued operation, and device disposal ability is large, the little occupation of land of size is few.
3, the solid waste selected has had very little granularity, avoids and pulverizes and grind the energy consumption brought.
4, be conveniently combined with power plant existing system, the quantities of transformation is little, and the equipment of increase also lacks.
5, carbonation reaction carries out under middle temperature 70-90 DEG C and low pressure (being no more than 2bar) condition, realizes quick carbonation reaction, can make CO in flue gas in 5 minutes while reducing energy consumption
2extrusion rate reaches 30%.
6, with other CO
2trapping technique is compared, and as organic aminated absorption process, its cost is at 250-350 yuan/ton of CO
2.And the decarburization cost of this technology is at 40-120 yuan/ton of CO
2.As can be deviate from the CO of in coal-fired plant flue gas 30% with lower cost
2also be very attractive.Flyash simultaneously after decarburization does not affect the original use approach of fly ash in electric power plant, is equivalent to raw material and does not consume, and still making cement additive and building materials can use, ignores so the cost of material of this decarbonization process can be similar to.
Accompanying drawing explanation
Fig. 1 is the utility model structural representation.
Detailed description of the invention
Embodiment of the present utility model is described in detail below in conjunction with drawings and Examples.
As shown in Figure 1, the fluidized system of a kind of direct trapping mineralising carbon dioxide in flue gas of the utility model, high calcium discarded object adopts fly ash in electric power plant, comprise: pretreatment unit 7, flue-gas temperature humidity adjustment unit 9, fluidized-bed reactor 10 and cyclone separator 11, raw coal is after coal pulverizer 1, burn in steam generator system 2, produce power delivers to turbine 3 and generator 4.Containing a large amount of flyash in the flue gas that burning produces, flue gas is after SCR reactor 5 denitration, again through electrostatic precipitator 6 dedusting, the flyash obtained is sent into pretreatment unit 7 and is carried out pretreatment, flue gas after dedusting again through FGD absorption tower 8 desulfurization, pretreatment reach standard after flyash deliver to fluidized-bed reactor 10 by induction system 12.Flue behind FGD absorption tower 8 arranges bypass, draws one flue gas to flue-gas temperature humidity adjustment unit 9, after regulating humiture wherein, be sent to fluidized-bed reactor 10.Flyash and flue gas haptoreaction in fluidized-bed reactor 10, achieves the goal.After reaction, the dusty gas going out fluidized-bed reactor 10 enters cyclone separator 11, completes gas solid separation wherein, and separating obtained gas is sent to flue gas main pipeline and discharges from chimney 13 and gas composition analysis instrument 16 can be utilized to analyze its composition.Wherein, temperature humidity regulon 9 comprises compressor 14 and the bubble tower 15 of liquid is housed.
In the utility model, pretreatment unit 7 gets flyash in the thin ash silo of power plant's electrostatic precipitator 6, or ships the high calcium such as slag, cement solid waste from outside.According to actual conditions, pretreatment unit 7 can comprise dry powder mill, adds thermal incinerator, stirred autoclave, filter press and rotary drum drier etc.Generally, first alkaline process desiliconization, uses stirred autoclave, filter press and rotary drum drier; Fine gtinding process again, selects dry powder grinder, last heat pre-treatment, uses and adds thermal incinerator.The raw material bucket of fluidized-bed reactor 10 is transported to through strength soot blower system through pretreated flyash or solid waste.
Flue-gas temperature humidity adjustment unit 9 is opened bypass from the flue after power plant desulphurization system and is extracted flue gas, and flue gas boosts to 0.2MPa through compressor 14.Flue gas enters the bubble tower 15 that liquid is housed again, and bubble tower 15 has heated for controlling temperature function, and that carrys out adjustments of gas by regulating the outlet pressure of flue gas takes moisture.The rear portion of flue-gas temperature humidity adjustment unit 9 is provided with humidity sensor and detects humidity value.To isothermal holding be done from the pipeline after bubble tower 15 and establish companion's heat to keep the humidity of flue gas.
The flue gas of coming from flue-gas temperature humidity adjustment unit 9 is blown into inside reactor from bottom through air distribution plate and blast cap by fluidized-bed reactor 10, is located at line continuous sampling mouth gets its CO of flue gas analysis at air inlet
2, SO
2concentration.The raw material bucket of fluid bed adopts strength to enter ash, can use N here
2or compressed air.Charging quantitatively enters from reactor lower part according to the program timing of setting, and by the flue gas fluidisation of bottom, fluidizing velocity is according to the diameter of particle and variable density.Fluidized-bed reactor 10 is according to the composition of different sample and active height, the diameter designing conversion zone and breeze way.Reacted dusty gas is taken out of from reactor head.
Dusty gas from fluidized-bed reactor 10 is carried out gas solid separation by cyclone separator 11, cyclone separator 11 carrys out design selection according to reacted product grain granularity, generally the solid of granularity 20 microns can be separated from gas, the pipeline after dedusting be established gas sample mouth on-line continuous analyze its CO
2, SO
2concentration.The bottom part of cyclone separator 11 from ash be product, a part of product can be rejoined raw material bucket to improve the carbonation reaction degree of CaO in raw material.
Pretreatment unit parameter recited above is as follows:
Described temperature humidity regulon parameter is as follows:
Described fluidized-bed reactor unit parameter is as follows:
Described cyclonic separation cell parameters is as follows:
Described on-line analysis cell parameters is as follows:
Utilize said system can realize directly trapping the fluidized-bed process of mineralising carbon dioxide in flue gas, a feasible process example is as follows:
The fluidized-bed process of direct trapping mineralising carbon dioxide in flue gas, use coal-powder boiler high-calcium fly ass to be raw material, CaO content is about 30%, and principal crystalline phase is mullite, quartzy and a large amount of vitreum amorphous Si O
2, D50 is 80 microns, and concrete steps are as follows:
The first step, finds that CaO is with CaSiO after analyzing ash sample
3form exists, and reactivity meets the demands, and for improving reactivity further, carries out fine gtinding process to flyash, and granularity being reduced to D50 is 20 microns, generally selects dry powder grinder, grinding 20min.Flyash can from power plant's ash silo strength soot blower system sample presentation.
Second step, the flue after power plant desulfurization is opened bypass and draw one flue gas, first through supercharger, pressure is brought up to 2bar, then adjusted by temperature and humidity regulator, temperature is adjusted to 90 degrees Celsius, and the adjustable range of humidity is 20%.
3rd step, introduced bottom fluidized-bed reactor by the flue gas mixing up temperature humidity and be blown into reactor through air distribution plate and blast cap, flyash adds from fluid bed underfeed mouth, and the charge proportion of solid and gas remains on 5kg flyash/m
3flue gas.Flyash is with flue gas upwards fluidisation, and fluidizing velocity 0.1m/s, keeps flyash time of staying in reactor to be 5min.Fluid bed top dusty gas is through cyclone dust collectors separating solids, and backflow flyash controls as 1:1.Get gaseous sample in the place of flue gas turnover fluidized system and survey wherein CO through flue gas analyzer
2and SO
2content, CO
27.5% is reduced to from about 12.3% concentration of entrance, and SO
2concentration is from 89mg/Nm
3be reduced to 21mg/Nm
3.
4th step, cyclone separator decarburization gas is out got back to former flue collector and is entered smoke stack emission, and the solid product be separated can be used to powder process coal ash cement, or as uses such as ground based fillers.
The utility model can utilize fly ash in electric power plant (also can use or add other high calcium solid waste) directly trapping mineralising carbon dioxide in flue gas, adopts the flyash CO directly and in flue gas after pretreatment with certain particle size
2fast reaction generates calcium carbonate.First, this technique directly utilizes basicity and the CO of flyash
2acid reaction, need not the metal cation such as calcium magnesium again in Ore Leaching raw material again adjust ph under alkalescence with CO
2reaction, technological process is shortened.In addition, use fluid bed can improve the treatment quantity in the unit interval to greatest extent, and reduces size and the occupation of land of equipment.Finally, this technique only needs to keep certain temperature and humidity just can carry out, and need not adopt high temperature and high pressure process conditions, reduce the energy consumption of process.Thus overcome traditional C O
2mineralization process long flow path, equipment size are large, energy consumption and the high shortcoming of cost.
Claims (4)
1. directly trap a fluidized system for mineralising carbon dioxide in flue gas, it is characterized in that, comprising:
Pretreatment unit (7), comprise dry powder mill for grinding and/or for heat add thermal incinerator and/or for the stirred autoclave of alkaline process desiliconization, filter press and rotary drum drier;
Flue-gas temperature humidity adjustment unit (9), is arranged in the bypass of flue, comprises the bubble tower (15) that liquid is housed, and the flue gas going out bypass enters bubble tower (15) and realizes temperature and humidity regulation;
Fluidized-bed reactor (10), picks out the solid material of pretreatment unit (7) and goes out the flue gas of flue-gas temperature humidity adjustment unit (9);
Cyclone separator (11), the dusty gas picking out fluidized-bed reactor (10) realizes gas solid separation, and wherein gained gas is delivered to flue and discharged from chimney (13).
2. directly trap the fluidized system of mineralising carbon dioxide in flue gas according to claim 1, it is characterized in that, described flue is disposed with SCR reactor (5) along flow of flue gas direction, electrostatic precipitator (6) and FGD absorption tower (8), described electrostatic precipitator (6) gained dust delivers to pretreatment unit (7) as solid material, electrostatic precipitator (6) gained flue gas enters FGD absorption tower (8) and carries out desulfurization, described bypass is arranged on the flue after desulfurization, compressor (14) is provided with in bypass, before compressor (14) is arranged at bubble tower (15).
3. directly trap the fluidized system of mineralising carbon dioxide in flue gas according to claim 1, it is characterized in that, a part for the solid product of described cyclone separator (11) is recycled to fluidized-bed reactor (10) and recycles.
4. directly trap the fluidized system of mineralising carbon dioxide in flue gas according to claim 1, it is characterized in that, the outlet conduit of described bubble tower (15) arranges attemperator.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104759203A (en) * | 2015-03-17 | 2015-07-08 | 华能国际电力股份有限公司 | Fluidized bed technology and fluidized bed system for directly capturing CO2 in mineralized flue gas |
| CN107469593A (en) * | 2017-08-28 | 2017-12-15 | 中国天辰工程有限公司 | Emission-control equipment and method during a kind of sial phosphorus molecular sieve drying and roasting |
| CN116492828A (en) * | 2023-04-18 | 2023-07-28 | 湖南工业大学 | Device for mineralizing and sealing carbon dioxide by using fly ash |
-
2015
- 2015-03-17 CN CN201520151601.2U patent/CN204522740U/en active Active
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104759203A (en) * | 2015-03-17 | 2015-07-08 | 华能国际电力股份有限公司 | Fluidized bed technology and fluidized bed system for directly capturing CO2 in mineralized flue gas |
| CN107469593A (en) * | 2017-08-28 | 2017-12-15 | 中国天辰工程有限公司 | Emission-control equipment and method during a kind of sial phosphorus molecular sieve drying and roasting |
| CN107469593B (en) * | 2017-08-28 | 2020-10-27 | 中国天辰工程有限公司 | Device and method for treating waste gas in drying and roasting process of silicon-aluminum-phosphorus molecular sieve |
| CN116492828A (en) * | 2023-04-18 | 2023-07-28 | 湖南工业大学 | Device for mineralizing and sealing carbon dioxide by using fly ash |
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