CN111750340A - Flue gas waste heat step recovery system and method thereof - Google Patents
Flue gas waste heat step recovery system and method thereof Download PDFInfo
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- CN111750340A CN111750340A CN202010550376.5A CN202010550376A CN111750340A CN 111750340 A CN111750340 A CN 111750340A CN 202010550376 A CN202010550376 A CN 202010550376A CN 111750340 A CN111750340 A CN 111750340A
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- waste heat
- temperature superheater
- flue gas
- temperature
- steam
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Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
- F22B1/00—Methods of steam generation characterised by form of heating method
- F22B1/02—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers
- F22B1/18—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers the heat carrier being a hot gas, e.g. waste gas such as exhaust gas of internal-combustion engines
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22D—PREHEATING, OR ACCUMULATING PREHEATED, FEED-WATER FOR STEAM GENERATION; FEED-WATER SUPPLY FOR STEAM GENERATION; CONTROLLING WATER LEVEL FOR STEAM GENERATION; AUXILIARY DEVICES FOR PROMOTING WATER CIRCULATION WITHIN STEAM BOILERS
- F22D1/00—Feed-water heaters, i.e. economisers or like preheaters
- F22D1/36—Water and air preheating systems
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22G—SUPERHEATING OF STEAM
- F22G1/00—Steam superheating characterised by heating method
- F22G1/16—Steam superheating characterised by heating method by using a separate heat source independent from heat supply of the steam boiler, e.g. by electricity, by auxiliary combustion of fuel oil
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22G—SUPERHEATING OF STEAM
- F22G5/00—Controlling superheat temperature
- F22G5/12—Controlling superheat temperature by attemperating the superheated steam, e.g. by injected water sprays
- F22G5/123—Water injection apparatus
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
- F23G7/04—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste liquors, e.g. sulfite liquors
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
- F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G2206/00—Waste heat recuperation
- F23G2206/10—Waste heat recuperation reintroducing the heat in the same process, e.g. for predrying
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G2206/00—Waste heat recuperation
- F23G2206/20—Waste heat recuperation using the heat in association with another installation
- F23G2206/203—Waste heat recuperation using the heat in association with another installation with a power/heat generating installation
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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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/12—Heat utilisation in combustion or incineration of waste
Abstract
A step recovery system and method for flue gas waste heat comprises an incinerator (100), a multi-stage superheater, a waste heat boiler (104), an air preheater (105), an economizer (106) and a fan (107), wherein corresponding flues are connected among the parts, a steam pipeline is connected between every two adjacent superheaters, a saturated steam inlet pipeline (311) is connected to the last superheater, and a high-temperature supersaturated steam outlet pipeline (314) is connected to the foremost superheater. According to the cascade recovery system for the flue gas waste heat, through researching and developing a flue gas waste heat recovery technology, heat of discharged high-temperature flue gas (1100-500 ℃) is used for producing supersaturated power steam, energy consumption of a project can be reduced, and running cost of the project is reduced.
Description
Technical Field
The invention relates to the field of waste gas and waste liquid incineration, in particular to a waste heat step recovery system of flue gas generated after waste gas and liquid incineration, which can be applied to a process for preparing Ethylene Glycol (EG) from coal, and a method for producing steam by recovering waste heat.
Background
The process for preparing the ethylene glycol from the coal generates a plurality of waste gas and liquid in the production process, the components are complex, the waste gas and liquid are treated as hazardous waste according to the regulations of hazardous waste identification standard inflammability (GB5085.4) and hazardous waste identification standard general rule (GB5085.7), and the hazardous waste incineration harmless treatment is required according to the regulations of hazardous waste incineration pollution control standard (GB 18484-2001).
The waste gas and waste liquid generated in the process production of preparing the ethylene glycol from the coal have higher general heat value, if a conventional incineration process is adopted, high-temperature flue gas generated after incineration is cooled by a spray tower and then is discharged through a draught fan and a chimney, and toxic and harmful substances in the waste gas and waste liquid are decomposed by incineration, but heat energy waste of different degrees is also caused.
Disclosure of Invention
In order to solve the technical problems, the invention provides a flue gas waste heat step recovery system and a method thereof, which can reduce the energy consumption of a project, and reduce the operation cost of the project by researching and developing a flue gas waste heat recovery technology to use the heat of the discharged high-temperature flue gas (1100-500 ℃) for producing supersaturated power steam.
The technical scheme adopted by the invention for solving the technical problems is as follows:
the utility model provides a flue gas waste heat step recovery system, is connected with between each parts and corresponds the flue including burning furnace, multistage over heater, exhaust-heat boiler, air heater, economizer and fan, is connected with steam pipeline between the adjacent over heater, is connected with saturated steam inlet pipeline on the last level over heater, is connected with high temperature supersaturation steam outlet pipeline on the over heater of the forefront.
The step recovery system for the waste heat of the flue gas comprises three superheaters, namely a high-temperature superheater, a medium-temperature superheater and a low-temperature superheater from front to back. Because the high-temperature heat exchanger has higher requirements on materials and higher manufacturing cost compared with the low-temperature heat exchanger, the method of using more low-temperature heat exchange materials and using less high-temperature heat exchange materials can be adopted to reduce the cost. Preferably, the area of the low-temperature superheater is larger than that of the medium-temperature superheater, and the area of the medium-temperature superheater is larger than that of the high-temperature superheater.
Furthermore, raw material steam enters the low-temperature superheater after sequentially passing through the inlet safety valve, the inlet electric valve, the upper hanging pipe header, the hanging pipe and the lower hanging pipe header, a middle-pass inlet header is arranged among the low-temperature superheater, the middle-temperature superheater and the high-temperature superheater, and a high-pass outlet header and an outlet electric valve are connected behind the high-temperature superheater.
Preferably, a first-stage water spray desuperheater is arranged between the low-temperature superheater and the middle-temperature superheater front middle-passing inlet header. And a secondary water spraying desuperheater is arranged between the high-temperature superheater and the middle-temperature superheater rear middle-passing inlet header. When the steam temperature exceeds the standard, the water spray desuperheater reduces the temperature of the superheated steam by spraying atomized water. The water spraying section is of a jacket structure, so that the rapid temperature change of the water mist evaporation section is prevented from causing metal thermal fatigue damage to the pipe wall.
According to the step recovery system for the flue gas waste heat, the coal economizer is externally connected with a coal economizer water inlet pipeline, a waste heat boiler water inlet pipeline is connected between the coal economizer and the waste heat boiler, and the waste heat boiler is further connected with a medium-pressure steam pipeline. The medium-pressure steam can be output to be delivered to a factory for use through the heat exchange of the economizer and the waste heat boiler.
According to the flue gas waste heat step recovery system, the air preheater is connected with an air inlet pipeline and a combustion air pipeline, and the other end of the combustion air pipeline is connected to the incinerator.
The method for applying the step recovery system for the waste heat of the flue gas comprises the steps that the flue gas generated by the incinerator sequentially passes through the high-temperature superheater, the medium-temperature superheater and the low-temperature superheater and then reaches the waste heat boiler, then passes through the air preheater and the economizer and then reaches a chimney through a fan to be discharged, and the raw material steam sequentially passes through the low-temperature superheater, the medium-temperature superheater and the high-temperature superheater to exchange heat and then outputs high-temperature supersaturated steam.
Further, the normal-temperature deoxygenated water reaches the economizer through the economizer water inlet pipeline for heat exchange, then reaches the waste heat boiler through the waste heat boiler water inlet pipeline for heat exchange, and finally outputs medium-pressure steam through the medium-pressure steam pipeline.
Furthermore, the combustion-supporting air reaches the air preheater through an air inlet pipeline at the air preheater, and reaches the incinerator through a combustion-supporting air pipeline after heat exchange, so as to provide oxygen for supporting combustion.
Compared with the prior art, the invention has the advantages that:
this flue gas waste heat cascade recovery system has preferably traditional flue gas waste heat recovery mode, makes the heat in the exhaust high temperature flue gas directly be used for heating saturated steam, is used for steam power generation with the high temperature supersaturated steam that finally generates, very big reduction energy resource consumption and running cost.
Drawings
The aspects and advantages of the present application will become apparent to those of ordinary skill in the art upon reading the following detailed description of the preferred embodiments. The drawings are only for purposes of illustrating the preferred embodiments and are not to be construed as limiting the invention.
In the drawings:
fig. 1 is a schematic process diagram of a step recovery system for flue gas waste heat in the embodiment 1;
the components represented by the reference numerals in the figures are:
100. incinerator, 101, high temperature superheater, 102, medium temperature superheater, 103, low temperature superheater, 104, waste heat boiler, 105, air preheater, 106, economizer, 107, fan, 300, supply line, 301, high temperature superheater front flue, 302, medium temperature superheater front flue, 303, low temperature superheater front flue, 304, waste heat boiler front channel, 305, air preheater front flue, 306, economizer front flue, 307, fan front flue, 308, chimney evacuation, 309, air inlet line, 310, combustion air line, 311, saturated steam inlet line, 312, low temperature supersaturated steam line, 313, medium temperature supersaturated steam line, 314, high temperature supersaturated steam outlet line, 315, economizer water inlet line, 316, waste heat boiler water inlet line, 317, medium pressure steam line.
Detailed Description
Exemplary embodiments of the present disclosure will be described in more detail below with reference to the accompanying drawings. It should be noted that these embodiments are provided so that this disclosure can be more completely understood and fully conveyed to those skilled in the art, and the present disclosure may be implemented in various forms without being limited to the embodiments set forth herein.
Example 1
Referring to fig. 1, the step recovery system for flue gas waste heat in the embodiment includes an incinerator 100, a multi-stage superheater, a waste heat boiler 104, an air preheater 105, an economizer 106, and a fan 107, and corresponding flues are connected between the components.
Further, the number of the superheaters is three, and from front to back, the superheaters are a high-temperature superheater 101, a medium-temperature superheater 102 and a low-temperature superheater 103. An intermediate temperature supersaturated steam pipeline 313 is connected between the high temperature superheater 101 and the intermediate temperature superheater 102, and a low temperature supersaturated steam pipeline 312 is connected between the intermediate temperature superheater 102 and the low temperature superheater 103. A saturated steam inlet pipeline 311 is connected to the low-temperature superheater 103, and a high-temperature supersaturated steam outlet pipeline 314 is connected to the high-temperature superheater 101.
Furthermore, the raw material steam is converted into high-temperature supersaturated steam after sequentially passing through an inlet safety valve, an inlet electric valve, an upper hanging pipe header, a hanging pipe, a lower hanging pipe header, a low-temperature superheater 103, a primary water-spraying desuperheater, a middle-pass inlet header, a middle-temperature superheater 102, a middle-pass inlet header, a secondary water-spraying desuperheater, a high-temperature superheater 101, a high-pass outlet header and an outlet electric valve.
In this embodiment, the primary and secondary spray attemperators function to reduce the superheated steam temperature by spraying atomized water when the steam temperature exceeds a standard. The water spraying section is of a jacket structure, so that the rapid temperature change of the water mist evaporation section is prevented from causing metal thermal fatigue damage to the pipe wall.
Preferably, a bypass is arranged behind the inlet safety valve, and when the incineration system goes wrong or redundant steam can enter the pressure-reducing and temperature-reducing device through the bypass to output medium-pressure saturated steam.
In this embodiment, an economizer water inlet line 315 is connected to the outside of the economizer 106, a waste heat boiler water inlet line 316 is connected between the economizer 106 and the waste heat boiler 104, and a medium pressure steam line 317 is further connected to the waste heat boiler 104. The heat exchange between the economizer 106 and the waste heat boiler 104 can output medium-pressure steam to be delivered to a factory for use.
In this embodiment, an air inlet line 309 and a combustion air line 310 are connected to the air preheater 105, and the other end of the combustion air line 310 is connected to the incinerator 100.
The step recovery system for flue gas waste heat of the embodiment is divided into four process flows in use, namely a flue gas process flow, a supersaturated steam process flow, a waste heat boiler steam process flow and an air preheating process flow.
The flue gas process flow is that fuel gas (natural gas, crude gas and the like), project waste gas, waste liquid and the like reach an incinerator 100 through a supply pipeline 300 to be fully combusted to generate flue gas, the temperature of the flue gas is about 1000 ℃, then the flue gas sequentially reaches a high-temperature superheater 101 through a high-temperature superheater front flue 301, the preferred temperature after heat exchange is 887.5 ℃, the flue gas passes through a medium-temperature superheater front flue 302 to reach a medium-temperature superheater 102, the preferred temperature after heat exchange is 745 ℃, the temperature after heat exchange reaches a low-temperature superheater 103 through a low-temperature superheater front flue 303, the preferred temperature after heat exchange is 500 ℃, the flue gas passes through a waste heat boiler front flue 304 to reach a waste heat boiler 104, the preferred temperature after heat exchange is 380 ℃, the flue gas passes through an air front flue 305 to reach an air preheater 105, the preferred temperature after heat exchange is 240 ℃, the flue gas before economizer front 306 to reach an economizer 106, and the exhaust is discharged through a chimney by a chimney exhaust 308 to reach the standard of the chimney.
The process flow of the supersaturated steam comprises the steps that saturated steam (with the enthalpy value of 2739.24MJ/t) with the raw material steam of 9.8MPa and 310 ℃ reaches the low-temperature superheater 103 through a saturated steam inlet pipeline 311 to exchange heat with flue gas to produce low-temperature supersaturated steam (with the enthalpy value of 3101.72MJ/t) with the flue gas of 9.8MPa and 400 ℃, medium-temperature supersaturated steam (with the enthalpy value of 3312.45MJ/t) with the flue gas is produced after reaching the medium-temperature superheater 102 through a low-temperature supersaturated steam pipeline 312 to exchange heat with the flue gas to produce high-temperature supersaturated steam (with the enthalpy value of 3478.95MJ/t) with the high-temperature superheater 101 and the flue gas of 9.8MPa and 540 ℃, and the high-temperature supersaturated steam is conveyed through a high-temperature supersaturated steam outlet pipeline 314 to serve as power steam for a plant.
The specific process parameters are shown in the following table:
preferably, the high-temperature heat exchanger has higher requirements on materials and higher manufacturing cost compared with the low-temperature heat exchanger, so that the cost can be reduced by adopting a method of using more low-temperature heat exchange materials and using less high-temperature heat exchange materials. The area of the low-temperature superheater 103 is larger than that of the medium-temperature superheater 102, and the area of the medium-temperature superheater 102 is larger than that of the high-temperature superheater 101. Preferably, when the supersaturated steam is produced, the low, medium and high superheated steam temperatures are 400 ℃, 475 ℃ and 570 ℃, respectively.
In the waste heat boiler steam process, normal-temperature deoxygenated water reaches the economizer 106 through an economizer water inlet pipeline 315 for heat exchange, the temperature of flue gas is raised to 104 ℃ after heat exchange, then the flue gas reaches the waste heat boiler 104 through a waste heat boiler water inlet pipeline 316 to produce saturated steam (with the enthalpy value of 2801.78MJ/t) of 3.8MPa and 273 ℃, and finally the medium-pressure steam is output through a medium-pressure steam pipeline 317 and is externally sent to a plant area for use.
In the air preheating process, combustion-supporting air required by the incinerator 100 reaches the air preheater 105 through an air inlet pipeline 309 at the air preheater 105, the temperature reaches 350 ℃ after heat exchange with flue gas, and the combustion-supporting air reaches the incinerator 100 through a combustion-supporting air pipeline 310 after heat exchange to provide oxygen for supporting combustion.
In conclusion, through improvement on flue gas waste heat recovery, the heat of the discharged high-temperature flue gas between 1100 ℃ and 500 ℃ is directly used for heating 9.8MPa saturated steam, so that the temperature of the discharged high-temperature flue gas reaches 540 ℃ and is used for steam power generation, and the energy consumption and the operation cost are greatly reduced.
Finally, it is to be noted that: in the above embodiments, the invention is not limited to the above embodiments in a reasonable manner, and persons skilled in the art to which the invention pertains will understand that all equivalent modifications and changes can be made without departing from the technical spirit of the invention and the scope of the invention is protected by the patent.
Claims (10)
1. The utility model provides a flue gas waste heat cascade recovery system, its characterized in that, including burning furnace (100), multistage over heater, exhaust-heat boiler (104), air heater (105), economizer (106) and fan (107), be connected with between each part and correspond the flue, be connected with the steam pipeline between the adjacent over heater, be connected with saturated steam inlet pipeline (311) on the last level over heater, be connected with high temperature supersaturation steam outlet pipeline (314) on the top over heater.
2. The stepped flue gas waste heat recovery system according to claim 1, wherein the number of the superheaters is three, namely a high-temperature superheater (101), a medium-temperature superheater (102) and a low-temperature superheater (103) from front to back.
3. The stepped flue gas waste heat recovery system according to claim 2, wherein the area of the low-temperature superheater (103) is larger than that of the medium-temperature superheater (102), and the area of the medium-temperature superheater (102) is larger than that of the high-temperature superheater (101).
4. The stepped recovery system for the waste heat of flue gas as recited in claim 2, wherein raw material steam sequentially passes through an inlet safety valve, an inlet electric valve, an upper hanging pipe header, a hanging pipe and a lower hanging pipe header and then enters the low-temperature superheater (103), a middle-passing inlet header is arranged among the low-temperature superheater (103), the middle-temperature superheater (102) and the high-temperature superheater (101), and a higher-passing outlet header and an outlet electric valve are connected behind the high-temperature superheater (101).
5. The stepped flue gas waste heat recovery system according to claim 4, wherein a first-stage water spray desuperheater is arranged between the low-temperature superheater (103) and the middle-temperature superheater (102) front middle passing inlet header. And a secondary water spray desuperheater is arranged between the high-temperature superheater (101) and the middle-temperature superheater (102) and a rear middle-inlet header.
6. The stepped flue gas waste heat recovery system according to claim 1, wherein a coal economizer water inlet pipeline (315) is connected outside the coal economizer (106), a waste heat boiler water inlet pipeline (316) is connected between the coal economizer (106) and the waste heat boiler (104), and a medium pressure steam pipeline (317) is further connected to the waste heat boiler (104).
7. The stepped flue gas waste heat recovery system as claimed in claim 1, wherein an air inlet line (309) and a combustion air line (310) are connected to the air preheater (105), and the other end of the combustion air line (310) is connected to the incinerator (100).
8. A method for applying the step recovery system of the flue gas waste heat according to any one of claims 1 to 7, characterized in that the flue gas generated by the incinerator (100) sequentially passes through the high-temperature superheater (101), the medium-temperature superheater (102) and the low-temperature superheater (103) and then reaches the waste heat boiler (104), then passes through the air preheater (105) and the economizer (106) and then reaches a chimney through a fan (107) to be discharged, and the raw material steam sequentially passes through the low-temperature superheater (103), the medium-temperature superheater (102) and the high-temperature superheater (101) to exchange heat and then outputs high-temperature supersaturated steam.
9. The step recovery method of flue gas waste heat according to claim 8, further comprising the steps of enabling normal-temperature deoxygenated water to reach the economizer (106) through an economizer water inlet pipeline (315) for heat exchange, enabling the normal-temperature deoxygenated water to reach the waste heat boiler (104) through a waste heat boiler water inlet pipeline (316) for heat exchange, and finally outputting medium-pressure steam through a medium-pressure steam pipeline (317).
10. The step recovery method for flue gas waste heat according to claim 8, further comprising the steps of enabling combustion air to reach the air preheater (105) through an air inlet pipeline (309) at the air preheater (105), and enabling the combustion air to reach the incinerator (100) through a combustion air pipeline (310) after heat exchange, so as to provide oxygen for supporting combustion.
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| CN202010550376.5A CN111750340A (en) | 2020-06-16 | 2020-06-16 | Flue gas waste heat step recovery system and method thereof |
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| CN202010550376.5A CN111750340A (en) | 2020-06-16 | 2020-06-16 | Flue gas waste heat step recovery system and method thereof |
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| CN201697137U (en) * | 2010-03-19 | 2011-01-05 | 吴道洪 | Waste incineration flue gas waste heat recovery device |
| CN104832896A (en) * | 2015-04-28 | 2015-08-12 | 江苏金源腾峰换热设备有限公司 | Incineration waste heat recovery device for blast furnace gas |
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| CN209688850U (en) * | 2019-02-20 | 2019-11-26 | 华西能源工程有限公司 | A kind of waste incineration waste heat recovery processing system |
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Application publication date: 20201009 |