CN105126572A - Flue gas mercury removing device, combustion system and flue gas mercury removing method - Google Patents
Flue gas mercury removing device, combustion system and flue gas mercury removing method Download PDFInfo
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- CN105126572A CN105126572A CN201510622719.3A CN201510622719A CN105126572A CN 105126572 A CN105126572 A CN 105126572A CN 201510622719 A CN201510622719 A CN 201510622719A CN 105126572 A CN105126572 A CN 105126572A
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Abstract
The invention relates to the field of flue gas treatment, and discloses a flue gas mercury removing device, a combustion system and a flue gas mercury removing method. The flue gas mercury removing device comprises mercury removing units (10), wherein the mercury removing units (10) are used for receiving flue gas and enabling elemental mercury in the flue gas to be fully oxidized by nitrogen oxide. According to the flue gas mercury removing device disclosed by the invention, a solid body which is insoluble in water is formed by enabling the elemental mercury in the flue gas to be fully oxidized by the nitrogen oxide, so that the removal of mercury in the flue gas is realized; due to the forming of a solid product, collecting and cleaning are easy, secondary pollution cannot be caused, pipeline equipment cannot be corroded, and the emission concentration of the mercury can meet the emission requirement of the mercury.
Description
Technical field
The present invention relates to fume treatment field, particularly, relate to a kind of flue gas mercury removal device, combustion system and flue gas hydrargyrum-removing method.
Background technology
Along with the development of economic society, people are concern for the environment problem more and more, for this reason for combustion system, the atmosphere pollutants emission standards of the flue gas demand fulfillment national regulation that boiler is discharged could discharge, such as, " fossil-fuel power plant atmospheric pollutant emission standard (GB13223-2011) " specifies, from 1 day January in 2015, execution mercury and mercuric compounds was less than 0.03mg/Nm by all electricity generation boilers
3concentration of emission limit value.
In prior art, usual use following methods carries out removing of mercury in flue gas, that is, use various demercuration adsorbent (as absorbent charcoal based, calcium base, flying dust base absorbant and some new adsorbents etc.) or various forms of deduster, SCR (SCR) denitrification apparatus and WFGD device etc. are installed.
But although said method all has certain function removing mercury in flue gas, for the coal that burning mercury content is higher, even if having employed these methods, the concentration of emission of mercury can not meet the requirement of above-mentioned concentration of emission limit value.Particularly for the oxygen-enriched combusting of coal dust, because oxygen-enriched combusting adopts flue gas recirculation, thus the mercury concentration in flue gas can be made higher than the concentration of flue gas in conventional air burning, the method for the existing like this mercury for removing flue gas in conventional air burning cannot meet the requirement of oxygen-enriched combusting flue gas demercuration.In addition, due to increasing substantially (dry flue gas can reach about 80%) of oxygen-enriched combusting carbon dioxide in flue gas concentration, use absorbent charcoal based, calcium base, flying dust base absorbant can produce stronger absorption/suction-operated to the carbon dioxide of high concentration, thus directly have influence on the adsorption/absorption effect of mercury in flue gas, but also the capture rate of oxygen-enriched combusting carbon dioxide can be caused to reduce.
Summary of the invention
The object of this invention is to provide a kind of flue gas mercury removal device, to overcome in prior art the problem that the concentration of emission that is difficult to meet mercury requires, the present invention also provides a kind of combustion system and flue gas hydrargyrum-removing method.
To achieve these goals, the invention provides a kind of flue gas mercury removal device, this flue gas mercury removal device comprises for receiving flue gas and making the Elemental Mercury in flue gas by the fully oxidized demercuration unit of nitrogen oxide.
Preferably, described demercuration unit comprises reactor and compressor, and the entrance of described compressor is used for passing into flue gas, and the outlet of described compressor is communicated with the entrance of described reactor.
Preferably, described demercuration unit comprises the first condenser be arranged between described compressor and described reactor.
Preferably, described demercuration unit comprises the gas-liquid separator with gas discharge outlet and liquid outlet, and described gas-liquid separator is arranged between described first condenser and described reactor.
Preferably, this flue gas mercury removal device comprises at least two the described demercuration unit be arranged in series.
Preferably, described reactor comprises superposed exhaust outlet and is positioned at the slag-drip opening of bottom, and the described entrance of described reactor is positioned at the middle part of described reactor.
Preferably, in adjacent two described demercuration unit, the entrance of a described demercuration unit is communicated with the described exhaust outlet of the reactor of demercuration unit described in another.
Preferably, this flue gas mercury removal device comprises circulating line, described demercuration unit comprises the first demercuration unit and the second demercuration unit that are arranged in series, the entrance of the reactor of described first demercuration unit is used for passing into flue gas, and the flue gas of discharging from described second demercuration unit to be circulated to described second demercuration unit demercuration again by described circulating line.
The present invention also provides a kind of combustion system, and this combustion system comprises boiler, and described combustion system also comprises described flue gas mercury removal device, and the demercuration unit of described flue gas mercury removal device is communicated with the flue gas discharge opening of described boiler.
Preferably, described combustion system is oxygen-enriched combustion system.
Preferably, described combustion system comprises and is connected to deduster between described boiler and described flue gas mercury removal device and the second condenser in turn.
The present invention also provides a kind of flue gas hydrargyrum-removing method, and this flue gas hydrargyrum-removing method comprises the following steps:
S: make the Elemental Mercury in flue gas fully oxidized by nitrogen oxide.
Preferably, described step S comprises: first compressed by flue gas before Elemental Mercury is fully oxidized by nitrogen oxide.
Preferably, described step S comprises: first carried out compressing and condensation by flue gas before Elemental Mercury is fully oxidized by nitrogen oxide.
Preferably, described step S comprises: first carried out successively by flue gas compressing before Elemental Mercury is fully oxidized by nitrogen oxide, condensation and gas-liquid separation.
Preferably, step S is repeatedly repeated until all removed by the mercury in flue gas.
Preferably, described step S comprises:
S1: flue gas is carried out respectively first compression, a condensation and a gas-liquid separation, then makes Elemental Mercury in flue gas by nitrogen oxides;
S2: reacted flue gas is carried out second-compressed, time condensation and secondary gas-liquid separation respectively, then makes the remaining Elemental Mercury in flue gas be again oxidized by nitrogen oxide;
S3: repeat step S2;
Wherein, when the concentration of nitrogen oxides in effluent is lower than 500ppm, the pressure limit of first compression and second-compressed is controlled as 10-15bar and 20-30bar;
When the concentration of nitrogen oxides in effluent is higher than 500ppm, the pressure limit of first compression and second-compressed is controlled as 5-10bar and 15-25bar.
The present invention is by making the Elemental Mercury in flue gas fully oxidized thus form water-fast solid and realize removing mercury in flue gas by nitrogen oxide, owing to being that therefore solid product easily collects removing, secondary pollution can not be caused, corrosion-free to pipe-line equipment, and the concentration of emission of mercury can meet its emission request.
Other features and advantages of the present invention are described in detail in detailed description of the invention part subsequently.
Accompanying drawing explanation
Accompanying drawing is used to provide a further understanding of the present invention, and forms a part for description, is used from explanation the present invention, but is not construed as limiting the invention with detailed description of the invention one below.In the accompanying drawings:
Fig. 1 is the structural representation of the flue gas mercury removal device that one embodiment of the present invention provide.
Fig. 2 is the structural representation of the flue gas mercury removal device that another embodiment of the invention provides.
Description of reference numerals
10: demercuration unit; 10a: the first demercuration unit;
10b: the second demercuration unit; 11: reactor;
11a: exhaust outlet; 11b: slag-drip opening;
12: compressor; 13: the first condensers;
14: gas-liquid separator; 14a: gas discharge outlet;
14b: liquid outlet; 20: circulating line;
30: blower fan.
Detailed description of the invention
Below in conjunction with accompanying drawing, the specific embodiment of the present invention is described in detail.Should be understood that, detailed description of the invention described herein, only for instruction and explanation of the present invention, is not limited to the present invention.
In the present invention, when not doing contrary explanation, the noun of locality such as " upper and lower, left and right " of use typically refers to reference to upper and lower, left and right shown in the drawings; " inside and outside " refers to profile inside and outside relative to each parts itself.
The present invention is based on the problem that concentration of emission that demercuration mode of the prior art is difficult to meet mercury requires and a kind of flue gas mercury removal device is provided.For a better understanding of the present invention, hereinafter with reference to accompanying drawing, the utility model is described in detail.
According to an aspect of the present invention, flue gas mercury removal device provided by the invention comprises for receiving flue gas and making the Elemental Mercury in flue gas by the fully oxidized demercuration unit 10 of nitrogen oxide.
The present invention is by making the Elemental Mercury in flue gas fully oxidized thus form water-fast solid (reaction principle of vide infra middle Elemental Mercury and nitrogen oxide) and realize removing mercury in flue gas by nitrogen oxide, owing to being that therefore solid product easily collects removing, secondary pollution can not be caused, corrosion-free to pipe-line equipment, and the concentration of emission of mercury can meet its emission request.
In addition, Elemental Mercury is as follows by the reaction principle of nitrogen oxides:
2NO(g)+O
2(g)→2NO
2(g)
2Hg(g)+2NO
2(g)→HgNO
2(g)+HgO(s)+NO(g)
HgNO
2(g)+NO
2(g)+O
2(g)→Hg(NO
3)
2
The net reaction of above-mentioned reaction: 2Hg (g)+2O
2(g)+NO (g)+NO
2→ HgO (s)+Hg (NO
3)
2
As depicted in figs. 1 and 2, described demercuration unit 10 can comprise reactor 11 and compressor 12, the entrance of described compressor 12 is used for passing into flue gas, the outlet of described compressor 12 is communicated with the entrance of reactor 11, make flue gas first compress pressurization by compressor 12 like this before entering reactor 11, thus enable the Elemental Mercury in flue gas fully oxidized by nitrogen oxide.It should be noted that, because reactor 11 needs the pressure bearing flue gas after overcompression, therefore generally reactor 11 is designed to voltage-resistant reactor (such as, withstand voltage about 20Mpa), in addition, in order to prevent the corrosion of reactor 11, the inwall of reactor 11 can be coated with antiacid coating or arrange teflon lined.
Wherein, because the temperature of flue gas flue gas after compressor 12 compresses can raise, and the efficiency of the higher demercuration of the temperature of flue gas is lower, and (such as, hot conditions is transformed into NO to NO
2reaction and Hg0 and NO
2between gas-phase reaction be all disadvantageous, the reaction principle see above), and, if temperature is too high, water vapour residual in flue gas can absorb sour gas thus form acid mist, is unfavorable for the safe operation of equipment, and the flue gas therefore after compression need be condensed to room temperature.Particularly, described demercuration unit 10 comprises the first condenser 13 be arranged between compressor 12 and reactor 11, thus can carry out condensation by the first condenser 13 to the flue gas after compression.In addition, because Elemental Mercury is carried out under normal temperature state by the reaction that nitrogen oxide is fully oxidized, the safe operation of whole device is not therefore affected.
In addition, described demercuration unit 10 comprises the gas-liquid separator 14 with gas discharge outlet 14a and liquid outlet 14b, described gas-liquid separator 14 is arranged between the first condenser 13 and reactor 11, gas-liquid separator 14 also has air inlet, gas discharge outlet 14a can be arranged on the top of gas-liquid separator 14, liquid outlet 14b can be arranged on the bottom of gas-liquid separator 14, and the air inlet of gas-liquid separator 14 can be arranged on the middle part of this gas-liquid separator 14, gas-liquid separator 14 is entered by described air inlet through the condensed flue gas of the first condenser 13, liquid after separation is got rid of by liquid outlet 14b, gas after separation is entered in reactor 11 by gas discharge outlet 14a.Why before flue gas enters reactor 11, carry out gas-liquid separation, be because prove through experiment, utilize Elemental Mercury (Hg
0) and nitrogen dioxide (NO
2) (the second point of reaction equation see in above-mentioned reaction principle) gas-phase reaction under high pressure removes the effect of mercury will far better than utilizing Elemental Mercury (Hg
0) in salpeter solution, react the effect removing mercury.That is, if do not carry out gas-liquid separation before flue gas enters reactor 11, then have part Elemental Mercury (Hg
0) and nitric acid reaction, thus with Elemental Mercury (Hg
0) and nitrogen dioxide (NO
2) gas-phase reaction formed " competition ", obviously this is unfavorable for the oxidation removal of mercury.
As one embodiment of the present invention, as shown in Figure 1, above-mentioned flue gas mercury removal device comprises at least two the demercuration unit 10 (shown in Fig. 1 is the situation comprising three demercuration unit 10) be arranged in series, and can improve demercuration efficiency further like this.
Wherein, described reactor 11 comprises superposed exhaust outlet 11a and is positioned at the slag-drip opening 11b of bottom, and the entrance of described reactor 11 is positioned at the middle part of reactor 11, thus is conducive to the discharge of reacting rear solid product.
When above-mentioned flue gas mercury removal device comprises at least two the demercuration unit 10 be arranged in series, in adjacent two demercuration unit 10, the entrance of a demercuration unit 10 is communicated with the exhaust outlet 11a of the reactor 11 of another demercuration unit 10.Elemental Mercury in flue gas in reactor 11 by nitrogen oxides after form solid product (i.e. mercury oxide and mercury salt), this solid product is got rid of by slag-drip opening 11b after sedimentation, and the flue gas after demercuration can enter another demercuration unit 10 by exhaust outlet 11a and carry out secondary demercuration.
As another embodiment of the invention, as shown in Figure 2, above-mentioned flue gas mercury removal device comprises circulating line 20, described demercuration unit 10 also comprises the first demercuration unit 10a and the second demercuration unit 10b that are arranged in series, the entrance of the reactor 11 of described first demercuration unit 10a is used for passing into flue gas, the flue gas of discharging from the second demercuration unit 10b to be circulated to the second demercuration unit 10b demercuration again by circulating line 20, thus provides demercuration efficiency.Wherein, circulating line 20 can arrange blower fan 30, thus make flue gas recirculation to the second demercuration unit 10b discharged from the second demercuration unit 10b.
According to another aspect of the present invention, the present invention also provides a kind of combustion system, and this combustion system comprises boiler, and described combustion system also comprises flue gas mercury removal device, and the demercuration unit 10 of this flue gas mercury removal device is communicated with the flue gas discharge opening of boiler.Wherein, described combustion system can be oxygen-enriched combustion system.
Wherein, described combustion system comprises and is connected to deduster between boiler and flue gas mercury removal device and the second condenser in turn.That is, first by deduster dedusting and by the second condenser condenses dehydration (water produced after condensation is discharged by the bottom of the second condenser) before flue gas enters mercury removal device, thus can ensure that the reliability service of the compression of follow-up carbon dioxide and liquefaction device is (in oxygen-enriched combustion system, a large amount of carbon dioxide can be produced in flue gas, in order to avoid a large amount of carbon dioxide impacts environment, generally can compress carbon dioxide, post liquefaction store).In addition, before flue gas enters mercury removal device, carry out dedusting, be in order to avoid resulting in blockage to subsequent pipeline, thus under high pressure produce serious safety problem.And first condensation dehydration was carried out by the second condenser before flue gas enters mercury removal device, because often containing a large amount of water vapours in oxygen-enriched combusting flue gas, if do not carry out condensation dehydration, a large amount of steam enters compression set, not only can affect the reliability service of compression device, also can make acid contaminant NOx, SO in flue gas
2etc. changing HNO into
3and H
2sO
4, these acidic materials all can cause serious corrosion to compressor, pipeline etc.
According to a further aspect of the invention, the present invention also provides a kind of flue gas hydrargyrum-removing method, and wherein, this flue gas hydrargyrum-removing method comprises the following steps: S: make the Elemental Mercury in flue gas fully oxidized by nitrogen oxide.
Wherein, described step S comprises: first compressed by flue gas before Elemental Mercury is fully oxidized by nitrogen oxide.Further, described step S comprises: first carried out compressing and condensation by flue gas before Elemental Mercury is fully oxidized by nitrogen oxide.Wherein, described step S comprises: first carried out successively by flue gas compressing before Elemental Mercury is fully oxidized by nitrogen oxide, condensation and gas-liquid separation.In addition, step S is repeatedly repeated until all removed by the mercury in flue gas.It should be noted that, compression above, condensation and gas-liquid separation can realize respectively by compressor, condenser and gas-liquid separator.
Further, described step S comprises: S1: flue gas is carried out respectively first compression, a condensation and a gas-liquid separation, then makes Elemental Mercury in flue gas by nitrogen oxides; S2: reacted flue gas is carried out second-compressed, time condensation and secondary gas-liquid separation respectively, then makes remaining Elemental Mercury in flue gas again by nitrogen oxides; S3: repeat step S2.Wherein, demercuration rate is directly proportional to nitrogen oxide (NOx) concentration in flue gas and reaction pressure, and therefore when nitrogen oxide (NOx) concentration is higher, the reaction pressure of reactor 11 can suitably reduce.Such as, when the concentration of nitrogen oxides in effluent is lower than 500ppm, the pressure limit of first compression and second-compressed is controlled as 10-15bar and 20-30bar; When the concentration of nitrogen oxides in effluent is higher than 500ppm, the pressure limit of first compression and second-compressed is controlled as 5-10bar and 15-25bar.
With specific embodiment, said method is described in detail below: as shown in Figure 1, from boiler furnace discharge flue gas respectively through dedusting, after condensation dehydration, enter in the compressor 12 of the first demercuration unit 10a and carry out first compression and be compressed to 10-15bar, a condensation is carried out and by near for the temperature of flue gas room temperature through first condenser 13 of the first demercuration unit 10a again from compressor 12 flue gas out, the liquid (water) produced is discharged by gas-liquid separator 14, (principle of demercuration is described in detail above to carry out demercuration process in the reactor 11 that flue gas after dehydration enters the first demercuration unit 10a, here no longer repeat), in reactor 11, a gaseous elemental mercury part in flue gas is converted into solid slag and is discharged by the slag-drip opening 11b of reactor 11 bottom, another part of gaseous elemental mercury in flue gas leaves the reactor 11 of the first demercuration unit 10a (generally with flue gas, first demercuration unit 10a mercury removal rate is 50-70%).Flue gas after preliminary demercuration enters in the compressor 12 of the second demercuration unit 10b and carries out second-compressed and be compressed to 20-30bar, time condensation is carried out and by near for the temperature of flue gas room temperature through first condenser 13 of the second demercuration unit 10b again from compressor 12 flue gas out, the liquid (water) produced is discharged by gas-liquid separator 14, carry out demercuration again in the reactor 11 that flue gas after dehydration enters the second demercuration unit 10b, the Elemental Mercury in flue gas is substantially completely removed substantially.Cause demercuration incomplete for avoiding system fluctuation, after compressing via the compressor 11 of the second demercuration unit 10b from the reactor 11 of the second demercuration unit 10b flue gas out by circulating line 20, the reactor 11 reentering the second demercuration unit 10b carries out demercuration again.In fact, proving through test, is the NO of 14bar, 500ppm and the O of 5% at pressure
2under existent condition, gas phase mercury simple substance (Hg
0) extrusion rate can reach more than 99%, approximate close to 100%.
Mercury removal device provided by the invention also has an advantage, and that is exactly that operating cost is low, because the flue gas of oxygen-enriched combusting itself needs the trapping through compressing and liquefying process implementation carbon dioxide, utilizes this special process process implementation gaseous state Hg
0and NO
xcooperation-removal, that is, mercury removal device provided by the invention can utilize existing device (such as compressor) in combustion system, has greatly saved the operating cost of oxygen-enriched combusting.Therefore, mercury removal device provided by the invention can realize the high efficiency, low cost of Elemental Mercury in flue gas and removes.
Below the preferred embodiment of the present invention is described in detail by reference to the accompanying drawings; but; the present invention is not limited to the detail in above-mentioned embodiment; within the scope of technical conceive of the present invention; can carry out multiple simple variant to technical scheme of the present invention, these simple variant all belong to protection scope of the present invention.
It should be noted that in addition, each the concrete technical characteristic described in above-mentioned detailed description of the invention, in reconcilable situation, can be combined by any suitable mode.In order to avoid unnecessary repetition, the present invention illustrates no longer separately to various possible combination.
In addition, also can be combined between various different embodiment of the present invention, as long as it is without prejudice to thought of the present invention, it should be considered as content disclosed in this invention equally.
Claims (17)
1. a flue gas mercury removal device, is characterized in that, this flue gas mercury removal device comprises for receiving flue gas and making the Elemental Mercury in flue gas by the fully oxidized demercuration unit (10) of nitrogen oxide.
2. flue gas mercury removal device according to claim 1, it is characterized in that, described demercuration unit (10) comprises reactor (11) and compressor (12), the entrance of described compressor (12) is used for passing into flue gas, and the outlet of described compressor (12) is communicated with the entrance of described reactor (11).
3. flue gas mercury removal device according to claim 2, is characterized in that, described demercuration unit (10) comprises the first condenser (13) be arranged between described compressor (12) and described reactor (11).
4. flue gas mercury removal device according to claim 3, it is characterized in that, described demercuration unit (10) comprises the gas-liquid separator (14) with gas discharge outlet (14a) and liquid outlet (14b), and described gas-liquid separator (14) is arranged between described first condenser (13) and described reactor (11).
5. according to the flue gas mercury removal device in claim 2-4 described in any one, it is characterized in that, this flue gas mercury removal device comprises at least two the described demercuration unit (10) be arranged in series.
6. flue gas mercury removal device according to claim 5, it is characterized in that, described reactor (11) comprises superposed exhaust outlet (11a) and is positioned at the slag-drip opening (11b) of bottom, and the described entrance of described reactor (11) is positioned at the middle part of described reactor (11).
7. flue gas mercury removal device according to claim 6, it is characterized in that, in adjacent two described demercuration unit (10), the entrance of a described demercuration unit (10) is communicated with the described exhaust outlet (11a) of the reactor (11) of demercuration unit (10) described in another.
8. according to the flue gas mercury removal device in claim 2-4 described in any one, it is characterized in that, this flue gas mercury removal device comprises circulating line (20), described demercuration unit (10) comprises the first demercuration unit (10a) and the second demercuration unit (10b) that are arranged in series, the entrance of the reactor (11) of described first demercuration unit (10a) is used for passing into flue gas, and the flue gas of discharging from described second demercuration unit (10b) to be circulated to described second demercuration unit (10b) demercuration again by described circulating line (20).
9. a combustion system, this combustion system comprises boiler, it is characterized in that, described combustion system also comprises the flue gas mercury removal device according to any one of claim 1-8, and the demercuration unit (10) of described flue gas mercury removal device is communicated with the flue gas discharge opening of described boiler.
10. combustion system according to claim 9, is characterized in that, described combustion system is oxygen-enriched combustion system.
11. combustion systems according to claim 9, is characterized in that, described combustion system comprises and is connected to deduster between described boiler and described flue gas mercury removal device and the second condenser in turn.
12. 1 kinds of flue gas hydrargyrum-removing methods, is characterized in that, this flue gas hydrargyrum-removing method comprises the following steps:
S: make the Elemental Mercury in flue gas fully oxidized by nitrogen oxide.
13., according to the flue gas hydrargyrum-removing method described in claim 12, is characterized in that, described step S comprises: first compressed by flue gas before Elemental Mercury is fully oxidized by nitrogen oxide.
14., according to the flue gas hydrargyrum-removing method described in claim 12, is characterized in that, described step S comprises: first carried out compressing and condensation by flue gas before Elemental Mercury is fully oxidized by nitrogen oxide.
15., according to the flue gas hydrargyrum-removing method described in claim 12, is characterized in that, described step S comprises: first carried out successively by flue gas compressing before Elemental Mercury is fully oxidized by nitrogen oxide, condensation and gas-liquid separation.
16., according to the flue gas hydrargyrum-removing method in claim 12-15 described in any one, is characterized in that, repeatedly repeat step S until all removed by the mercury in flue gas.
17. flue gas hydrargyrum-removing methods according to claim 12, is characterized in that, described step S comprises:
S1: flue gas is carried out respectively first compression, a condensation and a gas-liquid separation, then makes Elemental Mercury in flue gas by nitrogen oxides;
S2: reacted flue gas is carried out second-compressed, time condensation and secondary gas-liquid separation respectively, then makes the remaining Elemental Mercury in flue gas be again oxidized by nitrogen oxide;
S3: repeat step S2;
Wherein, when the concentration of nitrogen oxides in effluent is lower than 500ppm, the pressure limit of first compression and second-compressed is controlled as 10-15bar and 20-30bar;
When the concentration of nitrogen oxides in effluent is higher than 500ppm, the pressure limit of first compression and second-compressed is controlled as 5-10bar and 15-25bar.
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| CN108106044A (en) * | 2018-01-16 | 2018-06-01 | 天津大学建筑设计研究院 | Electric drive heat pump unit with smoke comprehensive processing function |
| CN111001292A (en) * | 2019-11-29 | 2020-04-14 | 上海理工大学 | Coal chemical looping combustion demercuration device and method |
| CN111001292B (en) * | 2019-11-29 | 2022-01-28 | 上海理工大学 | Coal chemical looping combustion demercuration device and method |
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