CN101670231A - Device and process for converting calcium process desulfurization into temperature difference crystallizing ammonia process desulfurization - Google Patents
Device and process for converting calcium process desulfurization into temperature difference crystallizing ammonia process desulfurization Download PDFInfo
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- CN101670231A CN101670231A CN200910068971A CN200910068971A CN101670231A CN 101670231 A CN101670231 A CN 101670231A CN 200910068971 A CN200910068971 A CN 200910068971A CN 200910068971 A CN200910068971 A CN 200910068971A CN 101670231 A CN101670231 A CN 101670231A
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- desulfurization
- desulfurizing tower
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- shower nozzle
- absorption liquid
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- 238000000034 method Methods 0.000 title claims abstract description 58
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 50
- 230000023556 desulfurization Effects 0.000 title claims abstract description 49
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 44
- 230000008569 process Effects 0.000 title claims abstract description 32
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 title claims abstract description 27
- 239000011575 calcium Substances 0.000 title claims abstract description 27
- 229910052791 calcium Inorganic materials 0.000 title claims abstract description 27
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 22
- 239000007788 liquid Substances 0.000 claims abstract description 66
- 238000002425 crystallisation Methods 0.000 claims abstract description 27
- 230000008025 crystallization Effects 0.000 claims abstract description 24
- 239000007921 spray Substances 0.000 claims abstract description 18
- 238000001035 drying Methods 0.000 claims abstract description 14
- 230000009469 supplementation Effects 0.000 claims abstract description 8
- 230000003009 desulfurizing effect Effects 0.000 claims description 56
- 238000010521 absorption reaction Methods 0.000 claims description 42
- 239000003546 flue gas Substances 0.000 claims description 26
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 23
- 239000007789 gas Substances 0.000 claims description 23
- 238000006243 chemical reaction Methods 0.000 claims description 20
- PQUCIEFHOVEZAU-UHFFFAOYSA-N Diammonium sulfite Chemical compound [NH4+].[NH4+].[O-]S([O-])=O PQUCIEFHOVEZAU-UHFFFAOYSA-N 0.000 claims description 17
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 claims description 15
- 229910052921 ammonium sulfate Inorganic materials 0.000 claims description 15
- 235000011130 ammonium sulphate Nutrition 0.000 claims description 15
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims description 12
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 12
- 238000005516 engineering process Methods 0.000 claims description 8
- AOSFMYBATFLTAQ-UHFFFAOYSA-N 1-amino-3-(benzimidazol-1-yl)propan-2-ol Chemical compound C1=CC=C2N(CC(O)CN)C=NC2=C1 AOSFMYBATFLTAQ-UHFFFAOYSA-N 0.000 claims description 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 6
- 229910052760 oxygen Inorganic materials 0.000 claims description 6
- 239000001301 oxygen Substances 0.000 claims description 6
- 238000000746 purification Methods 0.000 claims description 5
- 239000012141 concentrate Substances 0.000 claims description 4
- 238000001816 cooling Methods 0.000 claims description 3
- 238000001556 precipitation Methods 0.000 claims description 3
- 239000006228 supernatant Substances 0.000 claims description 3
- 238000005265 energy consumption Methods 0.000 abstract description 2
- 230000004048 modification Effects 0.000 abstract 1
- 238000012986 modification Methods 0.000 abstract 1
- 230000009466 transformation Effects 0.000 description 5
- 229910000831 Steel Inorganic materials 0.000 description 4
- 238000010276 construction Methods 0.000 description 4
- 230000007812 deficiency Effects 0.000 description 4
- 239000010959 steel Substances 0.000 description 4
- 239000002699 waste material Substances 0.000 description 4
- 238000005260 corrosion Methods 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 230000008439 repair process Effects 0.000 description 3
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 239000010808 liquid waste Substances 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 235000019738 Limestone Nutrition 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 230000002421 anti-septic effect Effects 0.000 description 1
- ZETCGWYACBNPIH-UHFFFAOYSA-N azane;sulfurous acid Chemical compound N.OS(O)=O ZETCGWYACBNPIH-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000003517 fume Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000007634 remodeling Methods 0.000 description 1
- 239000010802 sludge Substances 0.000 description 1
- 230000000638 stimulation Effects 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
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Abstract
The invention belongs to the technical field of environment protection, and relates to a device and a process for temperature difference crystallizing ammonia process desulfurization, which is especially suitable for the ammonia process modification and newly-built desulfurization of the original calcium process desulfurization device. The device comprises a desulfurization tower, a densifying device, a gas-liquid heat exchanger, a circulating pump, a concentration circulating pump, a magma pump, a concentration crystallization tank and a drying system, wherein the desulfurization tower, the circulating pump, the magma pump and the drying system adopt the devices in the original calcium process desulfurization; the lower part of the densifying device is provided with a gas distributor, andthe upper part thereof is provided with spray heads which are arranged in 2-3 layers; spray heads in the desulfurization tower are arranged in 2-4 layers, a liquid supplementation pipe is connected with the spray heads at the lowest layer in the desulfurization tower; the concentration crystallization tank is a tank with a conical bottom part; and the upper part of the concentration crystallization tank is provided with a pipeline to be connected with the bottom of the densifying device, the middle of the concentration crystallization tank is provided with a pipeline to be connected with theconcentration circulating pump, and the bottom is provided with a pipeline to be connected with the magma pump. The invention can farthest utilize the original devices on the premise of guaranteeing the normal desulfurization efficiency, thereby saving the investment, reducing the energy consumption and eliminating the secondary pollution.
Description
Technical field
The invention belongs to environmental technology field, relate to a kind of temperature difference crystallization ammonia desulfuration equipment and technology, be particularly useful for transformation or newly-built desulfurization that steam power plant's original calcium method desulfurizer changes ammonia process.
Background technology
At present, known calcium method (being limestone-based process) the sulfur removal technology waste liquid that has been in operation produces, and also has waste residues calcium sulfate to generate simultaneously, causes secondary pollution.And the ammonia process of desulfurization can not have waste liquid, waste sludge discharge, and the ammonium sulfate of generation can utilize.Therefore a lot of calcium method desulfurization change to the ammonia process of desulfurization of efficient and low power consuming.Expensive maximum is desulfurizing tower in the desulfurization of calcium method, because the difference of production technology, usually energy-conservation remodeling method is in original desulfurizing tower interior laminate layer, in tower, be divided into 2 intervals according to different concentration, but the height of desulfurizing tower seems not enough again after the layering, and steel construction undercapacity is originally transformed the anti-corrosion layer structure that also will inevitably destroy desulfurizing tower, and do not reach original antiseptic effect through the anticorrosive coat of repairing, transform very difficulty; Common ammonia desulfurizing process also exists ammonium sulfate in the absorption liquid easily in position crystallizations such as shower nozzle and pipelines and the problem that results in blockage.
Summary of the invention
In order to overcome the deficiency of prior art, solve the secondary pollution that the desulfurization of calcium method produces, and the steel construction undercapacity of the desulfurizing tower that exists in the desulfurizing tower transformation, the layer height deficiency, anticorrosive coat is difficult to repair, anti-corrosion material is Nai Gaore and thermal shocking etc. not, common ammonia desulfurizing process exists ammonium sulfate in the absorption liquid easily in position crystallizations such as shower nozzle and pipelines and the problem that results in blockage, the invention provides a kind of calcium method desulfurization changes the device and the technology of the temperature difference crystallization ammonia process of desulfurization, utilized original desulfurizing tower fully, circulating pump, the magma pump, drying system, do not change the desulfurizing tower internal structure, reach the stack gas cleaning discharging, do not cause the purpose of secondary pollution.
The device of the temperature difference crystallization ammonia process of desulfurization is changeed in calcium method desulfurization of the present invention, includes desulfurizing tower, enrichment device, gas-liquid heat-exchange, circulating pump, concentrates circulating pump, magma pump, condensing crystallizing groove, drying system; Desulfurizing tower, circulating pump, magma pump, drying system all are the equipment that has utilized in the desulfurization of original calcium method; Enrichment device bottom is provided with gas distributor, and its top is provided with shower nozzle, and shower nozzle is a layer 2-3; Shower nozzle in the desulfurizing tower is the layer 2-4 setting, and liquid supplementation pipe is connected with undermost shower nozzle in the desulfurizing tower; The condensing crystallizing groove is the tapered groove in bottom, can be by the purification tank for liquid waste transformation in the calcium method desulphurization plant, and its top has pipeline to be connected with enrichment device bottom, and the middle part has pipeline to be connected with concentrated circulating pump, and the bottom has pipeline to be connected with the magma pump.
The technological process of the calcium method desulfurization commentaries on classics temperature difference crystallization ammonia process of desulfurization of the present invention is as follows:
A. flue gas at first enters gas-liquid heat-exchange by advancing mouth, after flue gas is lowered the temperature, entering the enrichment device contacts with the absorption liquid that sprays by shower nozzle, sulfur dioxide in the flue gas and the ammoniacal liquor in the absorption liquid and sulfurous acid ammonia generation chemical reaction, generate ammonium sulfite and ammonium bisulfite etc. and be dissolved in the absorption liquid, flue gas is by preliminary purification like this; Flue gas is advanced mouth by tower and is entered desulfurizing tower then, and sulfur dioxide of flue gases continues to take place chemical reaction with ammoniacal liquor or ammonium sulfite in the absorption liquid that is ejected, and flue gas is by smart desulfurization like this, after exhaust outlet discharge.
B. absorption liquid is from the shower nozzle spray on desulfurizing tower top, with circulating pump absorption liquid is transported to shower nozzle in the desulfurizing tower and the shower nozzle in the enrichment device respectively from desulfurizing tower bottom, absorption liquid arrives desulfurizing tower bottom and enrichment device bottom from shower nozzle spray back, ammonium bisulfite in the absorption liquid is met ammoniacal liquor and is reduced into ammonium sulfite, the oxygen reaction that ammonium sulfite and gas distributor come out generates ammonium sulfate, the absorption liquid of enrichment device bottom flows into the condensing crystallizing groove, ammonium sulfate in the absorption liquid is carried out crystallisation by cooling, the precipitation and separate, the magma part is pumped into drying system by magma, supernatant partly is concentrated circulating pump and carries through the preliminary intensification of gas-liquid heat-exchange after the shower nozzle spray in the enrichment device, contact the also enrichment that further heats up with the flue gas in the enrichment device, move in circles.
C. ammoniacal liquor replenishes by liquid supplementation pipe undermost shower nozzle spray in desulfurizing tower.
D. oxic gas is pressurized is conveyed into bottom the desulfurizing tower and the gas distributor bottom the enrichment device, oxygen in the oxic gas and the reaction of the ammonium sulfite in the absorption liquid generate ammonium sulfate and are dissolved in the absorption liquid, the gas of not participating in reaction in the enrichment device advances mouth through tower and enters in the desulfurizing tower, does not participate in the gas of reaction and discharge through exhaust outlet in desulfurizing tower.
Because the present invention designs and adopted technique scheme, steel construction undercapacity, layer height deficiency, anticorrosive coat that having solved the desulfurization of calcium method effectively changes desulfurizing tower in the calcium method desulfurizing tower transformation that the temperature difference crystallization ammonia process of desulfurization exists are difficult to repair and the not high heat-proof problem of anti-corrosion material.It compared with prior art has following beneficial effect:
I. the temperature difference crystallization ammonia process of desulfurization is changeed in the desulfurization of calcium method, has eliminated secondary pollution, has improved environment protecting.
Ii. utilize original desulfurizing tower, circulating pump, magma pump, drying system etc., reduced cost;
Iii. add the enrichment device, avoid problem in the separate zone stimulation of desulfurizing tower, the problem includes: height deficiency, anticorrosive coat are difficult to repair and the problem of steel construction undercapacity;
Iv. adopt gas-liquid heat-exchange, effectively reduce the temperature of flue gas, desulfurizing tower need not increase the anti-high hot material of inwall can be used, thereby reduces improvement cost; The absorption liquid in the heat cycles simultaneously prevents that effectively the ammonium sulfate in the absorption liquid from resulting in blockage in position crystallization such as shower nozzle and pipeline, reduces maintenance cost;
V. adopt temperature difference crystallization processes, reach that need not to evaporate be the purpose of crystallization, saved energy consumption and evaporation equipment cost.
Description of drawings
The present invention is further described below in conjunction with drawings and Examples.
Fig. 1 is the apparatus structure and the process flow diagram of the embodiment of the invention.
Mark among the figure: 1-advances mouth, 2-gas-liquid heat-exchange, 3-enrichment device, 4-shower nozzle, 5-tower and advances mouth, 6-desulfurizing tower, 7-exhaust outlet, 8-circulating pump, 9-condensing crystallizing groove, 10-and concentrate circulating pump, 11-magma pump, 12-gas distributor, 13-liquid supplementation pipe, 14-drying system.
The specific embodiment
By shown in Figure 1, include desulfurizing tower (6), enrichment device (3), gas-liquid heat-exchange (2), circulating pump (8), concentrate circulating pump (10), magma pump (11), condensing crystallizing groove (9), drying system (14); Desulfurizing tower (6), circulating pump (8), magma pump (11), drying system (14) are the equipment that has utilized in the desulfurization of calcium method; Enrichment device (3) bottom is provided with gas distributor (12), and its top is provided with shower nozzle (4), and this shower nozzle (4) is a layer 2-3, uses pipeline to be connected with circulating pump (8) or gas-liquid heat-exchange (2) respectively; The shower nozzle (4) of desulfurizing tower (6) is the layer 2-4 setting, and the shower nozzle (4) in the desulfurizing tower (6) is connected with circulating pump (8) with pipeline, and liquid supplementation pipe (13) is connected with undermost shower nozzle (4) in the desulfurizing tower (6); Condensing crystallizing groove (9) is the tapered groove in bottom, can be by the flat purification tank for liquid waste transformation in the calcium method desulphurization plant, top has pipeline to be connected with enrichment device (3) bottom, and the middle part has pipeline to be connected with concentrated circulating pump (10), and the bottom has pipeline to be connected with magma pump (11).
The technological process of the calcium method desulfurization commentaries on classics temperature difference crystallization ammonia process of desulfurization of the present invention is as follows:
A. flue gas at first enters gas-liquid heat-exchange (2) by advancing mouth (1), flue gas is lowered the temperature, reduced fume high-temperature to enrichment device (3) and the resistant to elevated temperatures requirement of desulfurizing tower (6), flue gas enters enrichment device (3) and contacts with the absorption liquid that sprays by shower nozzle (4), sulfur dioxide in the flue gas, or the ammonium sulfite that generates with ammoniacal liquor generation chemical reaction in the absorption liquid, or generating ammonium bisulfite with ammonium sulfite reaction in the absorption liquid, flue gas is by preliminary purification like this; Flue gas is advanced mouth (5) by tower and is entered desulfurizing tower (6) then, and sulfur dioxide of flue gases continues to take place chemical reaction with ammoniacal liquor or ammonium sulfite in the absorption liquid that is ejected, like this flue gas by smart desulfurization after exhaust outlet (7) discharge.
B. absorption liquid is from shower nozzle (4) spray on desulfurizing tower (6) top, with circulating pump (8) absorption liquid is transported to interior shower nozzle (4) of desulfurizing tower (6) and the shower nozzle (4) in the enrichment device (3) respectively from desulfurizing tower (6) bottom, absorption liquid arrives desulfurizing tower (6) bottom and enrichment device (3) bottom from shower nozzle (4) spray back, ammonium bisulfite in the absorption liquid is met ammoniacal liquor and is reduced into ammonium sulfite, the oxygen reaction that ammonium sulfite and gas distributor (12) come out generates ammonium sulfate, the absorption liquid of enrichment device (3) bottom flows into condensing crystallizing groove (9), ammonium sulfate in the absorption liquid is carried out crystallisation by cooling, the precipitation and separate, the magma part is sent into drying system (14) generation ammonium sulfate by magma pump (11) and is utilized, supernatant partly is concentrated circulating pump (10) and carries process gas-liquid heat-exchange (2) tentatively to heat up after shower nozzle (4) spray in the enrichment device (3), contact the also enrichment that further heats up with the flue gas in the enrichment device (3), move in circles; Because absorption liquid is heated when (2) through gas-liquid heat-exchange, prevent that effectively the ammonium sulfate in the absorption liquid from resulting in blockage in position crystallization such as shower nozzle and pipeline, reduce maintenance cost.
C. ammoniacal liquor replenishes by undermost shower nozzle (4) spray of liquid supplementation pipe (13) in desulfurizing tower (6).
D. oxic gas is pumped to desulfurizing tower (6) bottom and enrichment device (3) bottom gas distributor (12), oxygen in the oxic gas and the reaction of the ammonium sulfite in the absorption liquid generate ammonium sulfate and are dissolved in the absorption liquid, the gas of not participating in reaction in enrichment device (3) advances mouth (5) through tower and enters in the desulfurizing tower (6), and the residual gas of not participating in reaction in desulfurizing tower (6) passes through exhaust outlet (7) discharging.
Claims (6)
1. the device of a calcium method desulfurization commentaries on classics temperature difference crystallization ammonia process of desulfurization is characterized in that: include desulfurizing tower, enrichment device, gas-liquid heat-exchange, circulating pump, concentrate circulating pump, magma pump, condensing crystallizing groove, drying system.
2. the device of the temperature difference crystallization ammonia process of desulfurization is changeed in calcium method desulfurization according to claim 1, and it is characterized in that: desulfurizing tower, circulating pump, magma pump, drying system all are the equipment that has utilized in the desulfurization of original calcium method.
3. the device of the temperature difference crystallization ammonia process of desulfurization is changeed in calcium method desulfurization according to claim 1, and it is characterized in that: enrichment device bottom is provided with gas distributor, and its top is provided with shower nozzle, and this shower nozzle is a layer 2-3.
4. the device of the temperature difference crystallization ammonia process of desulfurization is changeed in calcium method desulfurization according to claim 1, and it is characterized in that: the desulfurizing tower shower nozzle is the layer 2-4 setting, and liquid supplementation pipe is connected with undermost shower nozzle in the desulfurizing tower.
5. the device of the temperature difference crystallization ammonia process of desulfurization is changeed in calcium method desulfurization according to claim 1, it is characterized in that: the condensing crystallizing groove is the tapered groove in bottom, top has pipeline to be connected with enrichment device bottom, and the middle part has pipeline to be connected with concentrated circulating pump, and the bottom has pipeline to be connected with the magma pump.
One kind in the desulfurizer described in the claim 1, carry out the calcium method desulfurization technology of changeing the temperature difference crystallization ammonia process of desulfurization, it is characterized in that:
A. flue gas at first enters gas-liquid heat-exchange by advancing mouth, after flue gas is lowered the temperature, entering the enrichment device contacts with the absorption liquid that sprays by shower nozzle, sulfur dioxide in the flue gas, or the ammonium sulfite that generates with ammoniacal liquor generation chemical reaction in the absorption liquid, or generating ammonium bisulfite with ammonium sulfite reaction in the absorption liquid, flue gas is by preliminary purification like this; Flue gas is advanced mouth by tower and is entered desulfurizing tower then, and sulfur dioxide of flue gases continues to take place chemical reaction with ammoniacal liquor or ammonium sulfite in the absorption liquid that is ejected, like this flue gas by smart desulfurization after exhaust outlet discharge.
B. absorption liquid is from the shower nozzle spray on desulfurizing tower top, with circulating pump absorption liquid is transported to shower nozzle in the desulfurizing tower and the shower nozzle in the enrichment device respectively from desulfurizing tower bottom, absorption liquid arrives desulfurizing tower bottom and enrichment device bottom from shower nozzle spray back, ammonium bisulfite in the absorption liquid is met ammoniacal liquor and is reduced into ammonium sulfite, the oxygen reaction that ammonium sulfite and gas distributor come out generates ammonium sulfate, the absorption liquid of enrichment device bottom flows into the condensing crystallizing groove, ammonium sulfate in the absorption liquid is carried out crystallisation by cooling, the precipitation and separate, the magma part is pumped into drying system by magma, supernatant partly is concentrated circulating pump and carries through the preliminary intensification of gas-liquid heat-exchange after the shower nozzle spray in the enrichment device, contact the also enrichment that further heats up with the flue gas in the enrichment device, move in circles.
C. ammoniacal liquor replenishes by liquid supplementation pipe undermost shower nozzle spray in desulfurizing tower.
D. oxic gas is pressurized is conveyed into bottom the desulfurizing tower and the gas distributor bottom the enrichment device, oxygen in the oxic gas and the reaction of the ammonium sulfite in the absorption liquid generate ammonium sulfate and are dissolved in the absorption liquid, the gas of not participating in reaction in the enrichment device advances mouth through tower and enters in the desulfurizing tower, does not participate in the gas of reaction and discharge through exhaust outlet in desulfurizing tower.
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| CN2009100689719A CN101670231B (en) | 2009-07-23 | 2009-07-23 | Device and process for converting calcium process desulfurization into temperature difference crystallizing ammonia process desulfurization |
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| CN2009100689719A CN101670231B (en) | 2009-07-23 | 2009-07-23 | Device and process for converting calcium process desulfurization into temperature difference crystallizing ammonia process desulfurization |
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-
2009
- 2009-07-23 CN CN2009100689719A patent/CN101670231B/en active Active
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