CN202675913U - System for recovering waste heat of boiler flue gases with different parameters - Google Patents
System for recovering waste heat of boiler flue gases with different parameters Download PDFInfo
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- CN202675913U CN202675913U CN2012203351256U CN201220335125U CN202675913U CN 202675913 U CN202675913 U CN 202675913U CN 2012203351256 U CN2012203351256 U CN 2012203351256U CN 201220335125 U CN201220335125 U CN 201220335125U CN 202675913 U CN202675913 U CN 202675913U
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/25—Process efficiency
Abstract
The utility model relates to a system for recovering waste heat of boiler flue gases in different parameters. The system comprises a low-temperature flue gas system and a high-temperature flue gas system which are connected by a pipeline. The system for recovering waste heat of flue gases with two parameters utilizes the flue gases in different temperature ranges to heat, evaporate and overheat water and steam respectively to finally produce high-temperature and high-pressure steam with one parameter jointly. The system has the following advantages: the system utilizes the flue gases with various temperature parameters to heat water and steam respectively according to different temperature ranges; the flue gases above 240 DEG C are only used for overheating steam, and the flue gases with other parameters are respectively used for heating and evaporating water; the heat of the low-temperature flue gases can be indirectly and efficiently utilized by utilizing the system; and the produced high-temperature and high-pressure steam not only obtains better efficiency, but also avoids application to different types of steam turbines brought by various steam parameters, thus greatly reducing the complexity of a power generation system while improving the heat utilization efficiency.
Description
Technical field
The utility model relates to the waste heat recovery apparatus technical field, is specifically related to a kind of different parameters residual heat from boiler fume recovery system.
Background technology
Domestic metallurgy industry is the power consumption rich and influential family, the main electricity consumption alloy smelting of mineral hot furnace, and in the recent period because energy shortage, environmental requirement, domestic metallurgy industry is progressively being eliminated the old technology smelting that spreads the new technique.At present at home on a large scale metallurgical group ubiquity the electric furnace model different, the size two (many) that Gas Parameters does not wait is overlapped smelting system, the Gas Parameters of electric furnace generation also is not quite similar.Existing cogeneration technology only reclaims generating to a kind of parameter high-temperature flue gas waste heat, is difficult to the operating mode of taking into account the multiple type of furnace and depositing.Most metallurgical groups all exist the multiple electric furnace of different parameters, because existing heat recovery technology is difficult to take into account adjacent low-temperature furnace, have caused residual heat resources waste in various degree.
The utility model content
The technical solution adopted in the utility model is: a kind of different parameters residual heat from boiler fume recovery system, comprise two boilers that can produce the different parameters flue gas, and the low-temperature flue gas recovery system and the high-temperature flue gas recovery system that are connected with two boilers by pipeline respectively.
Above-mentioned a kind of different parameters residual heat from boiler fume recovery system, described low-temperature flue gas recovery system comprises the cryogenic system drum, and the cryogenic system economizer that is connected with the cryogenic system drum by pipeline respectively, cryogenic system evaporimeter, cryogenic system pendant superheater, described cryogenic system drum is connected with the main feed water pipe road by pipeline.
Above-mentioned a kind of different parameters residual heat from boiler fume recovery system, described high-temperature flue gas recovery system comprises the high-temperature systems drum, and the high-temperature systems economizer that is connected with the high-temperature systems drum by pipeline respectively, high-temperature systems evaporimeter, primary superheater, described primary superheater connects two-stage superheater by the vapor mixing header, described high-temperature systems drum is connected with the main feed water pipe road by pipeline, and the input of described vapor mixing header also is connected with the output of low-temperature flue gas recovery system.
Compared with prior art, the utility model has the advantages that:
The flue gas of the utility model patent utilization various temperature parameter divides the temperature range heating to water and steam respectively, and the flue gas more than 240 ℃ only is used for to steam superheating, and other parameter flue gases are used for respectively to feedwater heating and evaporation.Utilize native system indirectly low-temperature flue gas heat energy also efficiently to be utilized, the high temperature and high pressure steam of producing has not only obtained preferably efficient, also save simultaneously the application of the different model steam turbine that multiple steam parameter brings, when improving efficiency of utilization, greatly reduced numerous and diverse degree of electricity generation system.
Description of drawings
Fig. 1 is general structure schematic diagram of the present utility model.
Among the figure, 1, cryogenic system economizer 2, cryogenic system evaporimeter 3, cryogenic system drum 4, cryogenic system pendant superheater 5, jet chimney 6, high-temperature systems economizer 7, high-temperature systems evaporimeter 8, high-temperature systems drum 9, primary superheater 10, two-stage superheater 11, vapor mixing header 12, high parameter ferrosilicon furnace 13 low parameter ferrosilicon furnaces 14, main feed water pipe.
The specific embodiment
Below in conjunction with accompanying drawing the utility model is further described.
As shown in Figure 1, the boiler feedwater pipeline is transported to cryogenic system economizer 1 entrance and high-temperature systems economizer 6 entrances with 40 ℃ boiler main to two branch roads of moisture, the water of cryogenic system enters cryogenic system evaporimeter 2 after process low parameter ferrosilicon furnace 13 tail flue gas are heated to 190 ℃ in cryogenic system economizer 1, the steam water interface that cryogenic system evaporimeter 2 is produced enters cryogenic system drum 3 and separates the saturated vapor that obtains 1.7MPa, and the saturated vapor that cryogenic system drum 3 is separated enters to be superheated in advance in the cryogenic system pendant superheater 4 after 270 ℃ through pipe steam way 5 and is transported to vapor mixing header 11 in the high-temperature systems.The water of high-temperature systems enters high-temperature systems evaporimeter 7 after process high parameter ferrosilicon furnace 12 tail flue gas are heated to 190 ℃ in high-temperature systems economizer 6, the steam water interface that high-temperature systems evaporimeter 7 is produced enters high-temperature systems drum 8 and separates the saturated vapor that obtains 1.6MPa, high-temperature systems drum 8 separates the saturated vapor that obtains and enters to be superheated in the primary superheater 9 and be transported to vapor mixing header 11 after 260 ℃ and obtain 32t/h1.5MPa250 ℃ steam with the vapor mixing that the A system comes, enter two-stage superheater 10 from vapor mixing header 11 superheated steam out, be delivered to the steam turbine acting after the high-temperature flue gas with smoke inlet is superheated to 330 ℃.The flue gas of process Hot swapping enters smoke evacuation system and drains from chimney via air-introduced machine.
Take two 25000KV low temperature ferrosilicon furnaces and two 12500KV low temperature ferrosilicon furnaces as example, two 25000KLV low temperature ferrosilicon furnaces can produce 350 ℃ high-temperature flue gas 240000Nm
3/ h, two 12500KV low temperature ferrosilicon furnaces can produce 300 ℃ high-temperature flue gas 180000Nm
3/ h.This programme is according to different flue gas flow and Gas Parameters, less with exhaust gas volumn, the low-temperature flue gas system hypothermia that temperature is lower is produced 1.6MP low temperature, 270 ℃ superheated steam 16t/h, then be transported to the superheater entrance of high-temperature flue gas system high temperature through a pipeline, the inlet steam parameter is 1.5MP low temperature, 255 ℃, and 15.5t/h.The flue gas of high-temperature flue gas system can be divided into two temperature ranges and utilize respectively, utilize the interval 1.5MP of production low temperature below 290 ℃ of flue gas, the about 18t/h of 260 ℃ steam, this steam and low temperature cigarette system are for the 15.5t/h that comes, 1.5MP low temperature enters comprehensive superheater after 255 ℃ superheated steam converges, and utilizes the high temperature section flue gas with existing 1.5MP low temperature, 250 ℃, be transported to the steam turbine acting after the steam superheating to 330 of 32t/h ℃.
The above only is preferred implementation of the present utility model; should be understood that; for those skilled in the art; under the prerequisite that does not break away from the utility model know-why; can also make some improvements and modifications, these improvements and modifications also should be considered as protection domain of the present utility model.
Claims (3)
1. different parameters residual heat from boiler fume recovery system is characterized in that: comprise two boilers that can produce the different parameters flue gas, and the low-temperature flue gas recovery system and the high-temperature flue gas recovery system that are connected with two boilers by pipeline respectively.
2. a kind of different parameters residual heat from boiler fume recovery system according to claim 1, it is characterized in that: described low-temperature flue gas recovery system comprises the cryogenic system drum, and the cryogenic system economizer that is connected with the cryogenic system drum by pipeline respectively, cryogenic system evaporimeter, cryogenic system pendant superheater, described cryogenic system drum is connected with the main feed water pipe road by pipeline.
3. a kind of different parameters residual heat from boiler fume recovery system according to claim 1 and 2, it is characterized in that: described high-temperature flue gas recovery system comprises the high-temperature systems drum, and the high-temperature systems economizer that is connected with the high-temperature systems drum by pipeline respectively, high-temperature systems evaporimeter, primary superheater, described primary superheater connects two-stage superheater by the vapor mixing header, described high-temperature systems drum is connected with the main feed water pipe road by pipeline, and the input of described vapor mixing header also is connected with the output of low-temperature flue gas recovery system.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012203351256U CN202675913U (en) | 2012-07-12 | 2012-07-12 | System for recovering waste heat of boiler flue gases with different parameters |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012203351256U CN202675913U (en) | 2012-07-12 | 2012-07-12 | System for recovering waste heat of boiler flue gases with different parameters |
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| Publication Number | Publication Date |
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| CN202675913U true CN202675913U (en) | 2013-01-16 |
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| CN2012203351256U Expired - Fee Related CN202675913U (en) | 2012-07-12 | 2012-07-12 | System for recovering waste heat of boiler flue gases with different parameters |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104214755A (en) * | 2014-07-31 | 2014-12-17 | 盐城市锅炉制造有限公司 | Coke plant semi-coke dry-distillation low-temperature smoke waste heat utilizing method and system thereof |
| CN105020691A (en) * | 2015-07-29 | 2015-11-04 | 思安新能源股份有限公司 | Thermodynamic system of boiler |
-
2012
- 2012-07-12 CN CN2012203351256U patent/CN202675913U/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104214755A (en) * | 2014-07-31 | 2014-12-17 | 盐城市锅炉制造有限公司 | Coke plant semi-coke dry-distillation low-temperature smoke waste heat utilizing method and system thereof |
| CN104214755B (en) * | 2014-07-31 | 2015-12-23 | 江苏东九重工股份有限公司 | The blue charcoal destructive distillation low-temperature flue gas waste heat Application way of a kind of coke plant and system thereof |
| CN105020691A (en) * | 2015-07-29 | 2015-11-04 | 思安新能源股份有限公司 | Thermodynamic system of boiler |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20130116 Termination date: 20170712 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |