CN203771375U - Coal economizer for increasing flue-gas temperature at SCR system entrance - Google Patents
Coal economizer for increasing flue-gas temperature at SCR system entrance Download PDFInfo
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- CN203771375U CN203771375U CN201420098820.4U CN201420098820U CN203771375U CN 203771375 U CN203771375 U CN 203771375U CN 201420098820 U CN201420098820 U CN 201420098820U CN 203771375 U CN203771375 U CN 203771375U
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- Prior art keywords
- economizer
- scr
- gas temperature
- header
- flue
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 39
- 239000003546 flue gas Substances 0.000 title claims abstract description 39
- 239000003245 coal Substances 0.000 title claims abstract description 13
- 239000003054 catalyst Substances 0.000 claims abstract description 31
- 239000012530 fluid Substances 0.000 claims description 3
- 230000000694 effects Effects 0.000 abstract description 9
- 238000006243 chemical reaction Methods 0.000 abstract description 5
- 230000007613 environmental effect Effects 0.000 abstract description 3
- 230000001105 regulatory effect Effects 0.000 abstract 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract 1
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 4
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 3
- 239000000428 dust Substances 0.000 description 3
- 230000009471 action Effects 0.000 description 2
- 230000005540 biological transmission Effects 0.000 description 2
- 239000003517 fume Substances 0.000 description 2
- 230000008676 import Effects 0.000 description 2
- 238000000034 method Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- WWILHZQYNPQALT-UHFFFAOYSA-N 2-methyl-2-morpholin-4-ylpropanal Chemical compound O=CC(C)(C)N1CCOCC1 WWILHZQYNPQALT-UHFFFAOYSA-N 0.000 description 1
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 1
- 238000003916 acid precipitation Methods 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- BIGPRXCJEDHCLP-UHFFFAOYSA-N ammonium bisulfate Chemical compound [NH4+].OS([O-])(=O)=O BIGPRXCJEDHCLP-UHFFFAOYSA-N 0.000 description 1
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 1
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 1
- 235000011130 ammonium sulphate Nutrition 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000010531 catalytic reduction reaction Methods 0.000 description 1
- 230000001413 cellular effect Effects 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 238000001953 recrystallisation Methods 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 238000003466 welding Methods 0.000 description 1
Landscapes
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
- Chimneys And Flues (AREA)
Abstract
The utility model discloses a coal economizer for increasing the flue-gas temperature at an SCR system entrance. A branch pipe is arranged on a water supply pipeline connected with a coal economizer inlet header; the branch pipe is connected with the outlet pipe of the coal economizer outlet header; a single-way valve, a stop valve and a regulating valve are arranged on the branch pipe. According to the utility model, the opening degree of a branch valve is adjusted in a working condition with low loading, so as to reduce the heat exchange quantity of the coal economizer and flue gas and increase the flue-gas temperature at the exit of the coal economizer; the temperature increase of the coal economizer exit denotes that the reaction temperature of a SCR denitration system is increased; on one hand, the loading can meet the operation conditions of the SCR in a larger range; continuous operation time of the SCR denitration system in a power plant is increased; on the other hand, the activity of a SCR catalyst in the working condition with the low loading is increased; the denitration capacity of the SCR system is improved. Therefore, the power plant is assisted to better reach the index of environmental protection in a range of longer time.
Description
Technical field
The utility model relates to flue gas in power station boiler denitration field, specifically refers to a kind of economizer of the SCR of raising system entry flue-gas temperature.
Background technology
In fields such as boats and ships, motor vehicle and thermal power plants, engine or boiler combustion can produce nitrogen oxide NO
x, NO
xby NO, NO
2and N
2o composition is one of important sources of environmental pollution.These dusty gas are discharged in atmosphere, can bring the harm such as acid rain, photochemical fog, Ozone Layer Depletion, affect the mankind's life.SCR technology is under the effect of catalyst, and reactant is adsorbed on catalyst, generates the N harmless to the mankind
2and H
20, due to the existence of catalyst, denitration efficiency can reach very high level, and selective catalytic reduction (SCR) has become industrial most important denitration technology at present.
In recent years atmosphere pollutants emission standards day stricter, aspect thermal power plant, domestic requirements installs the retrofit work of SCR system additional to the active service unit of denitration device is not installed.The arrangement of SCR process system mainly comprises that high-temperature high dust is arranged, the low dirt of high temperature is arranged and the low dirt of low temperature is arranged, wherein high-temperature high dust is arranged and is adopted the most generally, SCR reactor is arranged between economizer and air preheater, this arrangement makes the flue-gas temperature that enters SCR denitrating system remain on 280 DEG C～420 DEG C, meet the active temperature interval of most catalyst, in active temperature interval, SCR system can obtain good effect, and denitration performance raises along with the rising of flue-gas temperature.But when flue-gas temperature is lower than prescribing a time limit under catalyst activity temperature range, catalyst activity is lower, makes one side denitration efficiency lower, and the escaping of ammonia rate is higher on the other hand, the NH of escape
3sO in meeting and flue gas
3reaction generates ammonium sulfate (NH4)
2sO
4with ammonium hydrogen sulfate NH4HSO4, when serious, can cause the obstruction of catalyst reaction passage and air downstream preheater.But when flue-gas temperature is higher than prescribing a time limit in catalyst activity temperature range, can make sintering of catalyst or recrystallization, reduce the service life of catalyst.
Consider the impact of temperature on SCR denitrating system and upstream device, the running temperature of SCR system generally designs at 300 DEG C～400 DEG C, and in this temperature range, catalyst can ensure to move under higher activity.Command because the generation load in power station is subject to dispatching of power netwoks, in peak times of power consumption, station boiler remains under BMCR or high load capacity operating mode and moves, and the inlet temperature of denitrification apparatus can ensure that denitrating system normally moves the putting into operation in temperature range of SCR.But station boiler heavy-duty service for a long time, at electricity consumption low peak period, electrical network is lower to the demand of power station generation load, station boiler moves under underload, now in SCR system, the reaction temperature of flue gas is lower, because the activity with temperature of catalyst reduces, therefore denitration efficiency is also lower.In addition, in the time that denitrification apparatus entrance flue gas temperature does not reach denitrating system and puts into operation lowest temperature, denitrating system is out of service, and the discharge capacity of nitrogen oxide increases, and power station is difficult to reach the environmental protection index of national regulation.Although catalyst quits work on the other hand, but still in the washing away of flue gas, flying dust does not reduce the wearing and tearing of catalyst, causes reduce the service life of catalyst.Therefore,, under Power Station Boiler in Low Loads operating condition, ensureing SCR denitrating system efficiency and improving the SCR denitrating system time of putting into operation is a difficult problem that needs solution in domestic denitration art.
Utility model content
Goal of the invention: in order to overcome the deficiencies in the prior art, the utility model provides a kind of economizer of the SCR of raising system entry flue-gas temperature.
Technical scheme: for solving the problems of the technologies described above, the economizer of a kind of SCR of raising system entry flue-gas temperature that the utility model provides, the SCR reactor that comprises housing, is located at the economizer exit header in housing, the economizer heat-exchanger rig being connected with economizer exit header, the economizer inlet header being connected with economizer heat-exchanger rig and is connected with housing bottom; Between described economizer inlet header and economizer exit header, be provided with a bypass duct, described bypass duct is provided with successively respectively one-way valve, stop valve and flow control valve on fluid flow direction.
Further, described SCR reactor comprises reactor shell, is located at the reserved layer of catalyst in reactor shell, the catalyst first floor and catalyst sublevel successively.
Further, described housing bottom is provided with an economizer hopper.
Further, the two ends of described bypass duct are respectively equipped with a three-way pipe connector, and bypass duct is connected by welding manner with intermediate header.
Further, described control valve is electronic control and regulation valve.
Further, described economizer heat-exchanger rig comprises one group of Coal Saver Hanged Pipe connected with economizer exit header, the economizer intermediate header being connected with each Coal Saver Hanged Pipe, the one group of economizer coiled pipe being connected with economizer intermediate header, and described economizer coiled pipe is connected with economizer inlet header.
Beneficial effect: the utility model just has the following advantages with respect to prior art:
The utility model is to utilize the heat exchange amount that regulates bypass valve door aperture to reduce economizer and flue gas under running on the lower load to improve economizer exit flue-gas temperature, the rising of economizer exit temperature means increase SCR denitrating system reaction temperature, make on the one hand load meet in a wider context the condition that SCR puts into operation, improve the SCR of power plant denitrating system continuous operating time, cause on the other hand the activity of SCR catalyst under running on the lower load to raise, SCR system denitration ability strengthens, thereby helps power plant within the longer time, to reach better environmental protection index.
Brief description of the drawings
Fig. 1 is structural representation of the present utility model.
Fig. 2 is bypass duct connection diagram of the present utility model.
Detailed description of the invention
Below in conjunction with accompanying drawing, the utility model is further described.
As depicted in figs. 1 and 2, improve an economizer for SCR system entry flue-gas temperature, comprise housing 20, be located at the economizer exit header 2 in housing 20, the one group of Coal Saver Hanged Pipe 3, the economizer intermediate header 4 being connected with each Coal Saver Hanged Pipe 3, the one group of economizer coiled pipe 5 being connected with economizer intermediate header 4, the economizer inlet header 6 being connected with economizer coiled pipe 5 that are connected with economizer exit header 2 and the SCR reactor being connected with housing 20 bottoms; Between described economizer inlet header 6 and economizer exit header 2, be provided with a bypass duct 10, described bypass duct 10 is provided with successively respectively one-way valve 9, stop valve 8 and flow control valve 7 on fluid flow direction; Described housing 20 bottoms are provided with an economizer hopper 12; Described SCR reactor comprises reactor shell 21, is located at the reserved layer 14 of catalyst in reactor shell 21, the catalyst first floor 15 and catalyst sublevel 16 successively.
Under boiler at low load operating condition, economizer import flue gas 1 enters economizer, economizer exit flue gas 11 temperature are lower than 300 DEG C, and between economizer exit and SCR reactor inlet, there is no heat transmission equipment, therefore SCR reactor inlet flue gas 13 temperature and economizer exit temperature approximately equal, lower than the put into operation lower limit of temperature range (being generally 300 DEG C～400 DEG C) of SCR system, now open branch road stop valve 8, and progressively increase control valve 7 valve openings and control the rate-of flow of branch road, due to the shunting action of bypass duct, the rate-of flow of participating in heat exchange can reduce, cause the heat exchange amount of medium and flue gas to reduce, therefore flue gas reduces at the thermal discharge in economizer surface region, economizer exit flue gas 11 and SCR import flue gas 13 temperature are raise and exceed 300 DEG C, reach the temperature range that puts into operation of SCR system, the operational percentage of SCR system and the effective storage life of catalyst are effectively improved.
A kind of method situation in the time of real work that improves running on the lower load SCR entrance flue gas temperature of the present utility model is as follows:
Boiler economizer heat-exchanger rig 17 comprises suspension type economizer tube 3, intermediate header 4, loop economizer pipe 5, under boiler at low load operating condition, economizer exit flue gas 11 temperature are lower than 300 DEG C, now open branch road stop valve 8, and progressively increase control valve 7 valve openings and control the rate-of flow of branch road, due to the shunting action of branch road, the rate-of flow of participating in heat exchange can reduce, cause the heat exchange amount of medium and flue gas to reduce, therefore flue gas reduces at the thermal discharge in economizer heat exchange region 17, thereby being raise, economizer exit flue-gas temperature exceedes 300 DEG C.The design of the SCR system temperature range that puts into operation is 300 DEG C～400 DEG C, three layers of catalyst of design in reactor, the first floor is reserved layer 14, reserved layer is below for being filled with two beds 15 and 16 of cellular catalyst, owing to there is no heat transmission equipment between economizer exit and SCR reactor inlet, therefore enter flue gas 13 temperature and the economizer exit temperature approximately equal of SCR ground floor catalyst 15, reach the temperature range that puts into operation of SCR system, effectively improved the operational percentage of SCR system and the effective storage life of catalyst.In addition, the thermal capacity of side medium is higher than fume side, in the time reducing identical heat exchange amount, the amplitude that fume side outlet temperature raises is greater than the amplitude that side medium outlet temperature reduces, therefore the impact on boiler economic operation economizer media outlet temperature being reduced is less, has ensured the operability of the utility model in engineering.The above is only preferred embodiment of the present utility model; be noted that for those skilled in the art; do not departing under the prerequisite of the utility model principle; can also make some improvements and modifications, these improvements and modifications also should be considered as protection domain of the present utility model.
Claims (6)
1. an economizer that improves SCR system entry flue-gas temperature, is characterized in that: the SCR reactor that comprises housing, is located at the economizer exit header in housing, the economizer heat-exchanger rig being connected with economizer exit header, the economizer inlet header being connected with economizer heat-exchanger rig and is connected with housing bottom; Between described economizer inlet header and economizer exit header, be provided with a bypass duct, described bypass duct is provided with successively respectively one-way valve, stop valve and flow control valve on fluid flow direction.
2. the economizer of raising according to claim 1 SCR system entry flue-gas temperature, is characterized in that: described SCR reactor comprises reactor shell, is located at the reserved layer of catalyst, the catalyst first floor and the catalyst sublevel in reactor shell successively.
3. the economizer of raising SCR system entry flue-gas temperature according to claim 1, is characterized in that: described housing bottom is provided with an economizer hopper.
4. the economizer of raising SCR system entry flue-gas temperature according to claim 1, is characterized in that: the two ends of described bypass duct are respectively equipped with a three-way pipe connector.
5. the economizer of raising SCR system entry flue-gas temperature according to claim 1, is characterized in that: described control valve is electronic control and regulation valve.
6. the economizer of raising SCR system entry flue-gas temperature according to claim 1, it is characterized in that: described economizer heat-exchanger rig comprises one group of Coal Saver Hanged Pipe connected with economizer exit header, the economizer intermediate header being connected with each Coal Saver Hanged Pipe, the one group of economizer coiled pipe being connected with economizer intermediate header, and described economizer coiled pipe is connected with economizer inlet header.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420098820.4U CN203771375U (en) | 2014-03-05 | 2014-03-05 | Coal economizer for increasing flue-gas temperature at SCR system entrance |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420098820.4U CN203771375U (en) | 2014-03-05 | 2014-03-05 | Coal economizer for increasing flue-gas temperature at SCR system entrance |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN203771375U true CN203771375U (en) | 2014-08-13 |
Family
ID=51288564
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201420098820.4U Expired - Lifetime CN203771375U (en) | 2014-03-05 | 2014-03-05 | Coal economizer for increasing flue-gas temperature at SCR system entrance |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN203771375U (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103900072A (en) * | 2014-03-05 | 2014-07-02 | 东南大学 | Economizer for improving temperature of smoke in inlet of SCR system |
| CN104819451A (en) * | 2015-04-03 | 2015-08-05 | 广东电网有限责任公司电力科学研究院 | Boiler economizer capable of controlling SCR inlet smoke temperature |
| CN107300189A (en) * | 2017-07-25 | 2017-10-27 | 浙江浙能绍兴滨海热电有限责任公司 | A kind of coal-fired combustion equipment |
-
2014
- 2014-03-05 CN CN201420098820.4U patent/CN203771375U/en not_active Expired - Lifetime
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103900072A (en) * | 2014-03-05 | 2014-07-02 | 东南大学 | Economizer for improving temperature of smoke in inlet of SCR system |
| CN104819451A (en) * | 2015-04-03 | 2015-08-05 | 广东电网有限责任公司电力科学研究院 | Boiler economizer capable of controlling SCR inlet smoke temperature |
| CN104819451B (en) * | 2015-04-03 | 2016-08-24 | 广东电网有限责任公司电力科学研究院 | A kind of boiler economizer that can control SCR inlet flue-gas temperature |
| CN107300189A (en) * | 2017-07-25 | 2017-10-27 | 浙江浙能绍兴滨海热电有限责任公司 | A kind of coal-fired combustion equipment |
| CN107300189B (en) * | 2017-07-25 | 2023-07-04 | 浙江浙能绍兴滨海热电有限责任公司 | Coal burning equipment |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term |
Granted publication date: 20140813 |