CN205032068U - Buggy oxygen boosting burning flue gas demercuration system - Google Patents
Buggy oxygen boosting burning flue gas demercuration system Download PDFInfo
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- CN205032068U CN205032068U CN201520543761.1U CN201520543761U CN205032068U CN 205032068 U CN205032068 U CN 205032068U CN 201520543761 U CN201520543761 U CN 201520543761U CN 205032068 U CN205032068 U CN 205032068U
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 96
- 239000003546 flue gas Substances 0.000 title claims abstract description 96
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 title claims abstract description 41
- 239000001301 oxygen Substances 0.000 title claims abstract description 41
- 229910052760 oxygen Inorganic materials 0.000 title claims abstract description 41
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 claims abstract description 44
- 229910052753 mercury Inorganic materials 0.000 claims abstract description 36
- 238000006243 chemical reaction Methods 0.000 claims abstract description 19
- 238000009833 condensation Methods 0.000 claims abstract description 16
- 230000005494 condensation Effects 0.000 claims abstract description 16
- 230000006835 compression Effects 0.000 claims abstract description 9
- 238000007906 compression Methods 0.000 claims abstract description 9
- 239000007788 liquid Substances 0.000 claims description 21
- 239000002817 coal dust Substances 0.000 claims description 13
- 239000000779 smoke Substances 0.000 claims description 6
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 abstract description 54
- 239000007787 solid Substances 0.000 abstract description 4
- 239000003344 environmental pollutant Substances 0.000 abstract description 3
- 239000007789 gas Substances 0.000 abstract description 3
- 231100000719 pollutant Toxicity 0.000 abstract description 3
- 238000007599 discharging Methods 0.000 abstract description 2
- 239000000126 substance Substances 0.000 abstract description 2
- 238000004140 cleaning Methods 0.000 abstract 1
- 238000003795 desorption Methods 0.000 abstract 1
- 238000000034 method Methods 0.000 description 22
- 238000005516 engineering process Methods 0.000 description 5
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 4
- 230000009102 absorption Effects 0.000 description 3
- 238000010521 absorption reaction Methods 0.000 description 3
- 239000003463 adsorbent Substances 0.000 description 3
- 238000002485 combustion reaction Methods 0.000 description 3
- 150000002730 mercury Chemical class 0.000 description 3
- 229910000474 mercury oxide Inorganic materials 0.000 description 3
- UKWHYYKOEPRTIC-UHFFFAOYSA-N mercury(ii) oxide Chemical compound [Hg]=O UKWHYYKOEPRTIC-UHFFFAOYSA-N 0.000 description 3
- 230000003647 oxidation Effects 0.000 description 3
- 238000007254 oxidation reaction Methods 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- 230000035484 reaction time Effects 0.000 description 3
- 230000004044 response Effects 0.000 description 3
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 239000002250 absorbent Substances 0.000 description 2
- 230000002745 absorbent Effects 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 229910052791 calcium Inorganic materials 0.000 description 2
- 239000011575 calcium Substances 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 239000003610 charcoal Substances 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 230000018044 dehydration Effects 0.000 description 2
- 238000006297 dehydration reaction Methods 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 238000004062 sedimentation Methods 0.000 description 2
- 239000002893 slag Substances 0.000 description 2
- 241000009298 Trigla lyra Species 0.000 description 1
- 239000000567 combustion gas Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000002803 fossil fuel Substances 0.000 description 1
- 229910052602 gypsum Inorganic materials 0.000 description 1
- 239000010440 gypsum Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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- Treating Waste Gases (AREA)
Abstract
The utility model relates to a power boiler atmospheric pollutants gas cleaning field discloses the demercuration system of an oxygen boosting burning flue gas. The system includes: the first compressor (C1) is configured as the flue gas compression pressurization of discharging the oxygen boosting burning, first condenser (H1) is configured as the warp flue gas condensation after the first compressor (C1) the compression pressurization, a high pressure reactor (R1), be configured as hold through flue gas reaction after first condenser (H1) the condensation, and the pipeline, be configured as and connect gradually the first compressor (C1) first condenser (H1) and a high pressure reactor (R1). Through above -mentioned technical scheme, high concentration nitrogen oxide and mercury in the oxygen boosting burning flue gas can fully reflect in high pressure reactor, generate stable solid -state mercuride, realize the quick desorption to simple substance mercury in the flue gas.
Description
Technical field
The utility model belongs to boiler of power plant atmosphere pollution filed of flue gas purification, particularly, relates to a kind of demercuration system of oxygen-enriched combusting flue gas.
Background technology
Coal burning is main artificial mercury emissions source.GB13223-2011 " fossil-fuel power plant atmospheric pollutant emission standard " 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.The coal-fired flue gas mercury removal technique and method developed at present, comprise and add various demercuration adsorbent as absorbent charcoal based, calcium base and flying dust base absorbant and some new adsorbents etc., or various forms of deduster, SCR (SCR) denitrating system and wet desulfurization of flue gas by limestone-gypsum method (WFGD) system etc. are installed, all there is certain function removing mercury in flue gas, but for the coal that burning mercury content is higher, even if having employed these technology or system, the concentration of emission of mercury can not meet the requirement of up-to-date concentration of emission limit value.And for the oxygen-enriched combustion technology of coal dust, owing to adopting flue gas recirculation, the mercury concentration in flue gas can be made higher than conventional air combustion product gases, and therefore, existing conventional air demercuration technology and system 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 coal dust oxygen-enriched combusting carbon dioxide in flue gas concentration, mercury absorptions/the adsorbents such as absorbent charcoal based, the calcium base of conventional air burning and flying dust base can be stronger to the carbon dioxide generation of high concentration absorption/suction-operated, thus directly have influence on the adsorption/absorption effect of mercury in flue gas, more can cause the reduction of oxygen-enriched combusting carbon capture rate.Therefore for prevent and treat the pollution of mercury to air from source, and ensure production safety, be badly in need of taking novel demercuration technology.
Utility model content
The purpose of this utility model is to provide a kind of equipment, and this equipment can carry out demercuration to coal dust oxygen-enriched combusting flue gas.
To achieve these goals, the utility model provides a kind of coal dust oxygen-enriched combusting flue gas mercury removal system, and this system comprises: the first compressor, is configured to the flue gas compressor pressurization of being discharged by oxygen-enriched combusting; First condenser, is configured to the flue gas condensing after described first compressor compresses pressurization; First high-pressure reactor, is configured to hold the smoke reaction after described first condenser condenses; And pipeline, be configured to connect described first compressor, described first condenser and described first high-pressure reactor successively.
Further, also connect the first gas-liquid separator between described first condenser and described first high-pressure reactor, the liquid that this first gas-liquid separator is configured to described first condenser condenses produces discharges described pipeline.
Further, this system also comprises: the second compressor, is configured to the flue gas compressor pressurization of being discharged by described first high-pressure reactor; Second condenser, is configured to the flue gas condensing after described second compressor compresses pressurization; Second high-pressure reactor, be configured to hold the smoke reaction after described second condenser condenses, wherein, the pressure in described second high-pressure reactor is greater than the pressure in described first high-pressure reactor; And described pipeline, be configured to connect described second compressor, described second condenser and described second high-pressure reactor successively.
Further, also connect the second gas-liquid separator between described second condenser and described second high-pressure reactor, the liquid that this second gas-liquid separator is configured to described second condenser condenses produces discharges described pipeline.
Further, this system also comprises blower fan, and the flue gas that this blower fan is configured to described second high-pressure reactor is discharged delivers to described second compressor.
Further, this system also comprises detector, be arranged on the exhaust opening of described first high-pressure reactor and/or described second high-pressure reactor, this detector is configured to the mercury content detected in the flue gas of described first high-pressure reactor and/or described second high-pressure reactor discharge.
Further, this system also comprises dedusting condenser, delivers to described first compressor after being configured to the flue gas ash removal condensation of being discharged by described oxygen-enriched combusting.
By technique scheme, the high concentration nitrogen oxide in oxygen-enriched combusting flue gas and mercury fully can reflect in high-pressure reactor, generate stable solid-state mercuride, realize the fast eliminating to Elemental Mercury in flue gas.
Other features and advantages of the utility model are described in detail in detailed description of the invention part subsequently.
Accompanying drawing explanation
Accompanying drawing is used to provide further understanding of the present utility model, and forms a part for description, is used from explanation the utility model, but does not form restriction of the present utility model with detailed description of the invention one below.In the accompanying drawings:
Fig. 1 is the coal dust oxygen-enriched combusting flue gas mercury removal system structural representation that the utility model embodiment provides;
Fig. 2 is the coal dust oxygen-enriched combusting flue gas hydrargyrum-removing method flow chart that the utility model embodiment provides.
Detailed description of the invention
Below in conjunction with accompanying drawing, detailed description of the invention of the present utility model is described in detail.Should be understood that, detailed description of the invention described herein, only for instruction and explanation of the utility model, is not limited to the utility model.
Fig. 1 is the coal dust oxygen-enriched combusting flue gas mercury removal system structural representation that the utility model embodiment provides.As shown in Figure 1, the coal dust oxygen-enriched combusting flue gas mercury removal system that the utility model provides can comprise: stage compressor C1, is configured to the flue gas compressor pressurization of being discharged by oxygen-enriched combusting; First-stage condenser H1, is configured to compress the flue gas condensing after pressurization by through stage compressor C1; One-level high-pressure reactor R1, is configured to hold through the condensed smoke reaction of first-stage condenser H1 (such as, reaction time can be 1s to 5min or to compress time of flue gas identical with compressor C1); And pipeline, be configured to connect stage compressor C1, first-stage condenser H1 and one-level high-pressure reactor R1 successively.In embodiments, can also connect one-level gas-liquid separator S1 between first-stage condenser H1 and one-level high-pressure reactor R1, this one-level gas-liquid separator S1 can be configured to liquid discharge tube road first-stage condenser H1 condensation produced.
Pass through technique scheme, oxygen-enriched combusting flue gas is utilized to need the feature compressed and liquefied, under high pressure, Elemental Mercury can react with nitrogen oxide (NOx) and generate stable, solid-state mercuride (such as, mercury salt, mercury oxide), mercury oxidation is fixed by the nitrogen oxide by the high concentration in oxygen-enriched combusting flue gas, thus realizes demercuration safely and efficiently.
The flue gas of oxygen-enriched combustion boiler discharge is after dedusting condensation, compress C1 by stage compressor to pressurize, one-level high-pressure reactor R1 is entered again after condensation dehydration, a gaseous mercury simple substance part is converted into solid slag and discharges by bottom one-level high-pressure reactor R1, and another part can leave one-level high-pressure reactor R1 with flue gas.According to utility model people actual measurement, in one-level high-pressure reactor R1, mercury removal rate is 50-70%.Said system also comprises dedusting condenser (not shown), delivers to stage compressor C1 after being configured to the flue gas ash removal condensation of being discharged by oxygen-enriched combusting.
In a preferred embodiment, in order to demercuration more fully, the oxygen-enriched combusting flue gas mercury removal system that the utility model provides can adopt the combination of many group the said equipments.Such as, adopt the mode of classification that the combination of many group the said equipments is set.In such embodiment, said system can also comprise: split-compressor C2, is configured to the flue gas compressor pressurization of being discharged by one-level high-pressure reactor R1; Secondary condenser H2, is configured to compress the flue gas condensing after pressurization by through split-compressor C2; Secondary high-pressure reactor R2, be configured to hold through the condensed smoke reaction of secondary condenser H2 (such as, reaction time can be 1s to 5min or to compress time of flue gas identical with compressor C2), wherein, the pressure in secondary high-pressure reactor R2 is greater than the pressure in one-level high-pressure reactor R1; And described pipeline, be configured to connect described split-compressor C2, described secondary condenser H2 and described secondary high-pressure reactor R2 successively.In embodiments, similar to embodiment above, can connect secondary gas-liquid separator S2 between secondary condenser H2 and secondary high-pressure reactor R2, this secondary gas-liquid separator S2 is configured to liquid discharge tube road secondary condenser H2 condensation produced.
By technique scheme, the flue gas after preliminary demercuration, by split-compressor C2 second compression again, enters secondary high-pressure reactor R2 after condensation dehydration, and gaseous elemental mercury can carry out reacting with nitrogen oxide and be substantially completely removed in secondary high-pressure reactor R2.
In preferred embodiment, cause demercuration incomplete for avoiding system fluctuation, can also arrange closed circuit after secondary high-pressure reactor R2, the flue gas after demercuration can enter split-compressor C2 through closed circuit, carries out again demercuration reaction after compression in secondary high-pressure reactor R2.In such embodiment, this system can also comprise blower fan P1, and this blower fan P1 is arranged in above-mentioned closed circuit, delivers to split-compressor C2 for the flue gas of being discharged by secondary high-pressure reactor R2.
In embodiments, the course of reaction of next stage is needed to carry out when can detect and determine that mercury content judges by the flue gas of discharging one-level high-pressure reactor R1 and secondary high-pressure reactor R2.Further, system can also comprise detector, be arranged on the exhaust opening of one-level high-pressure reactor H1 and/or secondary high-pressure reactor H2, this detector is configured to the mercury content detected in the flue gas of one-level high-pressure reactor H1 and/or secondary high-pressure reactor H2 discharge.Such as, when the mercury content in the flue gas that one-level high-pressure reactor H1 discharges is non-vanishing, flue gas is continued pass into split-compressor C2; For another example, when the mercury content in the flue gas that secondary high-pressure reactor H2 discharges is non-vanishing, flue gas is continued circulation and pass into split-compressor C2, or next stage compressor (not shown) again.It should be noted that, the pipeline of the oxygen-enriched combusting flue gas mercury removal system provided at the utility model is provided with valve, with the trend of flue gas in control piper and the reaction time etc. in high-pressure reactor.
Oxygen-enriched combusting flue gas is after above-mentioned multistage (such as, secondary) high-pressure reactor, and demercuration rate can reach 100%.It should be noted that, demercuration rate is directly proportional to the NOx concentration in flue gas and reaction pressure, and therefore when NOx concentration is higher, the reaction pressure of high-pressure reactor can suitably reduce.With 500ppm concentration for boundary, when NOx concentration in flue gas is lower than 500ppm, the pressure limit of a split-compressor is controlled as 10-15bar and 20-30bar; When NOx concentration is higher than 500ppm, the pressure limit of a split-compressor can be controlled as 5-10bar and 15-25bar.Because the efficiency of the higher demercuration of flue-gas temperature is lower, the flue gas after compression need be condensed to room temperature.
Continue with reference to figure 1.The flue gas that oxygen-enriched combusting burner hearth is discharged is after dedusting condensation, and can be compressed to 10-15bar by stage compressor C1, then be down to room temperature through condenser H1, the liquid (such as, water) of generation can be discharged by gas-liquid separator S1.Gas after compression enters reaction in one-level high-pressure reactor R1, and the gaseous elemental mercury of 50-70% can be solid-state mercury oxide and mercury salt by NOx oxidation transformation, discharges after sedimentation by bottom one-level high-pressure reactor R1.Flue gas after demercuration can be compressed to 20-30bar again by split-compressor C2, dewater to room temperature through secondary condenser H2 and secondary gas-liquid separator S2, enter secondary high-pressure reactor R2 again, mercury after reaction in flue gas can 100% to remove, and solid slag can be discharged by R2 bottom secondary high-pressure reactor.If demercuration is incomplete, flue gas reenters secondary high-pressure reactor R2 and carries out secondary response again, to ensure that the mercury in flue gas is substantially completely removed after compressing via split-compressor C2 by closed circuit.
Reaction in high-pressure reactor as shown in formula (1)-(6), Elemental Mercury under gaseous state with reaction of nitrogen oxides; Simultaneously for improving the reaction rate of reaction (1), the oxygen concentration in flue gas should be greater than 2%.
formula (1)
formula (2)
2Hg (g)+O
2(g) → 2HgO (s) formula (3)
Hg (g)+NO
2(g) → 2HgO (s)+NO (g) formula (4)
Hg (g)+NO
2(g) → Hg (NO2) (s) formula (5)
Hg (g)+N
2o
4(g) → Hg (N
2o
4) (s) formula (6).
Another aspect of the present utility model, additionally provides a kind of coal dust oxygen-enriched combusting flue gas hydrargyrum-removing method, such as, can the system that provides of composition graphs 1 use.Fig. 2 is the coal dust oxygen-enriched combusting flue gas hydrargyrum-removing method flow chart that the utility model embodiment provides.As shown in Figure 2, the coal dust oxygen-enriched combusting combustion gas demercuration method that the utility model embodiment provides can comprise: S201, and the flue gas discharged by oxygen-enriched combusting compresses pressurization by stage compressor C1; S202, will compress the flue gas after pressurization by first-stage condenser H1 condensation by stage compressor C1; And S203 will by first-stage condenser H1 condensed flue gas input one-level high-pressure reactor R1, and make flue gas react (such as, first scheduled time) in this one-level high-pressure reactor R1.Pass through technique scheme, under high pressure, Elemental Mercury can react with nitrogen oxide (NOx) and generate stable, solid-state mercuride (such as, mercury salt, mercury oxide), mercury oxidation is fixed by the nitrogen oxide by the high concentration in oxygen-enriched combusting flue gas, thus realizes demercuration safely and efficiently.In embodiments, said method can also comprise: deliver to stage compressor C1 again after the first dedusting condensation of the flue gas discharged by oxygen-enriched combusting.
In a preferred embodiment, can be realized flue gas demercuration more completely by the step of repeatedly carrying out said method, in such embodiment, said method can also comprise: the flue gas of being discharged by one-level high-pressure reactor R1 compresses pressurization by split-compressor C2; The flue gas after pressurization will be compressed by secondary condenser H2 condensation by split-compressor C2; Will by secondary condenser H2 condensed flue gas input secondary high-pressure reactor R2, and flue gas is reacted (such as in this secondary high-pressure reactor R2, second scheduled time), wherein, the pressure in this secondary high-pressure reactor R2 can be greater than the pressure in one-level high-pressure reactor R1.
Further, said method also comprises: detect the mercury content in the flue gas of secondary high-pressure reactor R2 discharge; And when described mercury content exceedes predetermined value, the flue gas of being discharged by secondary high-pressure reactor R2 is sent into split-compressor C2 and is again circulated.
The technique scheme that the utility model provides, adopt two stages of compression device (i.e. compressor) and high-pressure reactor (i.e. one-level high-pressure reactor R1 and secondary high-pressure reactor R2), realize the quick and complete of Elemental Mercury in flue gas by the high concentrate NOx in high-response pressure and oxygen-enriched combusting flue gas and remove.
The flue gas hydrargyrum-removing method of current routine of comparing, the demercuration method that the utility model proposes has following advantage:
1, demercuration efficiency is high; After two-stage (or multistage) compressive reaction, demercuration rate can reach 100%.
2, waste pollutant easily processes; Form water-fast solid after Elemental Mercury and NOx react, easily collect removing after sedimentation, can not secondary pollution be caused.
3, operating cost is low; Oxygen-enriched combusting flue gas itself needs, through compressing and liquefying the trapping of process implementation carbon, to utilize this technical process to realize gaseous state Hg
0with the cooperation-removal of NOx, without the need to installing independent mercury removal device in addition additional, do not increase energy consumption newly at oxygen-enriched combusting, the method does not use any consumptive material simultaneously, and thus operating cost is low.
4, use safety; Reaction is carried out under normal temperature state, and influential system does not run.Reactant is gaseous state, and product is water-fast solid-state, is corrosion-free to pipe-line equipment.
Below preferred embodiment of the present utility model is described by reference to the accompanying drawings in detail; but; the utility model is not limited to the detail in above-mentioned embodiment; within the scope of technical conceive of the present utility model; can carry out multiple simple variant to the technical solution of the utility model, these simple variant all belong to protection domain of the present utility model.Such as, split-compressor and high-pressure reactor can be changed into three grades or level Four.
It should be noted that in addition, each concrete technical characteristic described in above-mentioned detailed description of the invention, in reconcilable situation, can be combined by any suitable mode, such as between one-level high-pressure reactor and stage compressor, increase closed circuit and arrange blower fan, the flue gas for being discharged by one-level high-pressure reactor is delivered to stage compressor and is carried out circular response.In order to avoid unnecessary repetition, the utility model illustrates no longer separately to various possible combination.
In addition, also can be combined between various different embodiment of the present utility model, as long as it is without prejudice to thought of the present utility model, it should be considered as content disclosed in the utility model equally.
Claims (6)
1. a coal dust oxygen-enriched combusting flue gas mercury removal system, is characterized in that, this system comprises:
First compressor (C1), is configured to the flue gas compressor pressurization of being discharged by oxygen-enriched combusting;
First condenser (H1), is configured to the flue gas condensing after described first compressor (C1) compression pressurization;
First high-pressure reactor (R1), is configured to hold through the condensed smoke reaction of described first condenser (H1);
Second compressor (C2), is configured to the flue gas compressor pressurization of described first high-pressure reactor (R1) being discharged;
Second condenser (H2), is configured to the flue gas condensing after described second compressor (C2) compression pressurization;
Second high-pressure reactor (R2), be configured to hold through the condensed smoke reaction of described second condenser (H2), the pressure in wherein said second high-pressure reactor (R2) is greater than the pressure in described first high-pressure reactor (R1); And
Pipeline, be configured to connect described first compressor (C1), described first condenser (H1) and described first high-pressure reactor (R1) successively, and connect described second compressor (C2), described second condenser (H2) and described second high-pressure reactor (R2) successively.
2. system according to claim 1, it is characterized in that, also connect the first gas-liquid separator (S1) between described first condenser (H1) and described first high-pressure reactor (R1), the liquid that this first gas-liquid separator (S1) is configured to described first condenser (H1) condensation produces discharges described pipeline.
3. system according to claim 1, it is characterized in that, also connect the second gas-liquid separator (S2) between described second condenser (H2) and described second high-pressure reactor (R2), the liquid that this second gas-liquid separator (S2) is configured to described second condenser (H2) condensation produces discharges described pipeline.
4. system according to claim 3, it is characterized in that, this system also comprises blower fan (P1), and this blower fan (P1) is configured to the flue gas that described second high-pressure reactor (R2) is discharged to deliver to described second compressor (C2).
5. system according to claim 1, it is characterized in that, this system also comprises detector, be arranged on the exhaust opening of described first high-pressure reactor (R1) and/or described second high-pressure reactor (R2), this detector is configured to detect the mercury content in the flue gas that described first high-pressure reactor (R1) and/or described second high-pressure reactor (R2) discharge.
6. system according to claim 1, is characterized in that, this system also comprises dedusting condenser, delivers to described first compressor (C1) after being configured to the flue gas ash removal condensation of being discharged by described oxygen-enriched combusting.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104971596A (en) * | 2015-07-24 | 2015-10-14 | 中国神华能源股份有限公司 | Demercuration system and method for pulverized coal oxygen-enriched combustion smoke |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104971596A (en) * | 2015-07-24 | 2015-10-14 | 中国神华能源股份有限公司 | Demercuration system and method for pulverized coal oxygen-enriched combustion smoke |
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