CN113446863B - A system and method for comprehensive utilization of waste heat in coking production process - Google Patents
A system and method for comprehensive utilization of waste heat in coking production process Download PDFInfo
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- CN113446863B CN113446863B CN202110551279.2A CN202110551279A CN113446863B CN 113446863 B CN113446863 B CN 113446863B CN 202110551279 A CN202110551279 A CN 202110551279A CN 113446863 B CN113446863 B CN 113446863B
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- 239000002918 waste heat Substances 0.000 title claims abstract description 58
- 238000004939 coking Methods 0.000 title claims abstract description 29
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 23
- 238000000034 method Methods 0.000 title claims abstract description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 172
- 238000010791 quenching Methods 0.000 claims abstract description 49
- 230000000171 quenching effect Effects 0.000 claims abstract description 49
- 239000000571 coke Substances 0.000 claims abstract description 34
- 238000011084 recovery Methods 0.000 claims abstract description 29
- 239000012528 membrane Substances 0.000 claims abstract description 11
- 239000003034 coal gas Substances 0.000 claims abstract 5
- 229920006395 saturated elastomer Polymers 0.000 claims description 31
- 239000007789 gas Substances 0.000 claims description 25
- 239000000203 mixture Substances 0.000 claims description 22
- 230000005611 electricity Effects 0.000 claims description 9
- 239000007921 spray Substances 0.000 claims description 9
- 230000009467 reduction Effects 0.000 claims description 7
- 238000000926 separation method Methods 0.000 claims description 6
- 238000010438 heat treatment Methods 0.000 claims description 4
- 230000009471 action Effects 0.000 claims description 3
- 239000000498 cooling water Substances 0.000 claims description 3
- 238000012423 maintenance Methods 0.000 claims 1
- 238000005265 energy consumption Methods 0.000 abstract description 5
- 230000008901 benefit Effects 0.000 abstract description 3
- 230000000694 effects Effects 0.000 abstract description 3
- 238000010248 power generation Methods 0.000 abstract 2
- 238000011033 desalting Methods 0.000 description 10
- 230000000630 rising effect Effects 0.000 description 10
- 230000001174 ascending effect Effects 0.000 description 4
- 238000005507 spraying Methods 0.000 description 3
- 230000017525 heat dissipation Effects 0.000 description 2
- 238000007731 hot pressing Methods 0.000 description 2
- 238000003303 reheating Methods 0.000 description 2
- 238000009834 vaporization Methods 0.000 description 2
- 230000008016 vaporization Effects 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
- F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
- F27D17/10—Arrangements for using waste heat
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01D—NON-POSITIVE DISPLACEMENT MACHINES OR ENGINES, e.g. STEAM TURBINES
- F01D13/00—Combinations of two or more machines or engines
- F01D13/02—Working-fluid interconnection of machines or engines
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01D—NON-POSITIVE DISPLACEMENT MACHINES OR ENGINES, e.g. STEAM TURBINES
- F01D15/00—Adaptations of machines or engines for special use; Combinations of engines with devices driven thereby
- F01D15/10—Adaptations for driving, or combinations with, electric generators
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
- F01K11/00—Plants characterised by the engines being structurally combined with boilers or condensers
- F01K11/02—Plants characterised by the engines being structurally combined with boilers or condensers the engines being turbines
-
- 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
- F22B1/1892—Systems therefor not provided for in F22B1/1807 - F22B1/1861
-
- 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
- F22D1/50—Feed-water heaters, i.e. economisers or like preheaters incorporating thermal de-aeration of feed-water
-
- 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
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22G—SUPERHEATING OF STEAM
- F22G7/00—Steam superheaters characterised by location, arrangement, or disposition
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
- F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
- F27D17/10—Arrangements for using waste heat
- F27D17/15—Arrangements for using waste heat using boilers
-
- 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
-
- 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
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
-
- 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
- Y02P80/00—Climate change mitigation technologies for sector-wide applications
- Y02P80/10—Efficient use of energy, e.g. using compressed air or pressurized fluid as energy carrier
- Y02P80/15—On-site combined power, heat or cool generation or distribution, e.g. combined heat and power [CHP] supply
Landscapes
- Engineering & Computer Science (AREA)
- General Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- Physics & Mathematics (AREA)
- Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Environmental & Geological Engineering (AREA)
- Thermal Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Sustainable Development (AREA)
- Sustainable Energy (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Engine Equipment That Uses Special Cycles (AREA)
Abstract
本发明涉及一种焦化生产过程余热综合利用系统及方法，所述系统包括干熄焦余热回收系统及荒煤气余热回收系统；干熄焦余热回收系统包括除盐水箱、汽轮发电机组及干熄焦锅炉；汽轮发电机组包括依次连接的高压缸、中低压缸和发电机；干熄焦锅炉包括锅炉汽包，以及自下至上依次设置于干熄焦锅炉本体内的省煤器、膜式水冷器及蒸发器、一次再热器、二次再热器、一次过热器和二次过热器；荒煤气余热回收系统包括上升管第一汽包、第一上升管换热器、上升管第二汽包及第二上升管换热器；本发明能够最大限度的提高焦化余热利用率，降低企业吨焦能耗；同时采用超高温超高压机组发电，提高发电量，经济效益及节能降耗效果显著。
The present invention relates to a system and method for comprehensive utilization of waste heat in a coking production process, the system comprising a dry coke quenching waste heat recovery system and a raw coal gas waste heat recovery system; the dry coke quenching waste heat recovery system comprises a desalted water tank, a steam turbine generator set and a dry coke quenching boiler; the steam turbine generator set comprises a high-pressure cylinder, a medium-low-pressure cylinder and a generator connected in sequence; the dry coke quenching boiler comprises a boiler drum, and an economizer, a membrane water cooler and an evaporator, a primary reheater, a secondary reheater, a primary superheater and a secondary superheater arranged in the dry coke quenching boiler body from bottom to top; the raw coal gas waste heat recovery system comprises a first riser drum, a first riser heat exchanger, a second riser drum and a second riser heat exchanger; the present invention can maximize the utilization rate of coking waste heat and reduce the energy consumption per ton of coke in the enterprise; at the same time, ultra-high temperature and ultra-high pressure units are used for power generation to increase power generation, and the economic benefits and energy-saving and consumption-reducing effects are remarkable.
Description
Technical Field
The invention relates to the technical field of coking production waste heat recovery, in particular to a comprehensive waste heat utilization system and method in a coking production process.
Background
At present, waste heat recovery measures commonly adopted by coking enterprises comprise raw coke gas waste heat recovery and red coke waste heat recovery, wherein the raw coke gas waste heat recovery utilizes a coke oven riser to exchange heat to generate low-pressure saturated steam for a low-pressure steam user, and the red coke waste heat recovery utilizes a dry quenching boiler to generate high-temperature high-pressure superheated steam for a steam turbine generator set to generate power, and the raw coke gas waste heat recovery and the red coke waste heat recovery are relatively independent.
To further accelerate transformation and upgrading of the coking industry and promote technical progress of the coking industry, promote comprehensive utilization rate of resources and energy-saving and environment-friendly level, and promote high-quality development of the coking industry. According to the invention, two production process systems of raw gas waste heat recovery and red coke waste heat recovery are organically combined, according to the waste heat utilization characteristics and waste heat steam parameters of each process system and according to the energy utilization principle of 'quality-based energy utilization, temperature opposite and cascade utilization', the problems of waste heat dissipation, high-parameter steam temperature and pressure reduction and the like are avoided, the waste heat utilization rate is improved to the greatest extent, and the ton coke energy consumption of enterprises is reduced.
Disclosure of Invention
The invention provides a comprehensive utilization system and method of waste heat in a coking production process, which can furthest improve the utilization rate of the coking waste heat, reduce the ton coke energy consumption of enterprises, simultaneously adopt an ultrahigh temperature and ultrahigh pressure unit to generate electricity, improve the generated energy and have remarkable economic benefit, energy conservation and consumption reduction effects.
In order to achieve the above purpose, the invention is realized by adopting the following technical scheme:
the coking production process waste heat comprehensive utilization system comprises a dry quenching waste heat recovery system and further comprises a raw gas waste heat recovery system, wherein the dry quenching waste heat recovery system comprises a desalting water tank, a turbo generator set and a dry quenching boiler, the turbo generator set comprises a high-pressure cylinder, a medium-low pressure cylinder and a generator which are sequentially connected, the dry quenching boiler comprises a boiler steam drum, and an economizer, a membrane water cooler, an evaporator, a primary reheater, a secondary reheater, a primary superheater and a secondary superheater which are sequentially arranged in a dry quenching boiler body from bottom to top, the raw gas waste heat recovery system comprises a first riser steam drum, a first riser heat exchanger, a second riser heat drum and a second riser heat exchanger, and the specific structure is as follows:
The desalted water outlet of the desalted water tank is sequentially connected with a deoxidized water supply pump, a water supply preheater and a deoxidizer through a desalted water outlet pipeline, wherein the water supply preheater is arranged at a circulating gas outlet of the dry quenching boiler; the deaeration water outlet of the deaerator is respectively connected with the inlet of a boiler feed pump and the inlet of a steam drum feed pump, the outlet of the boiler feed pump is connected with the water inlet of an economizer in a dry quenching boiler, the water outlet of the economizer is connected with the water inlet of a boiler steam drum, the water outlet of the boiler steam drum is connected with the steam-water mixture inlet of the boiler steam drum through a membrane water cooler and an evaporator, the saturated steam outlet of the boiler steam drum is sequentially connected with the steam inlet of a high-pressure cylinder in a steam turbine generator unit through a primary superheater and a secondary superheater, the steam outlet of the high-pressure cylinder is connected with a primary reheater and a secondary reheater through a steam pipeline, the secondary reheater is connected with the steam inlet of a middle-low pressure cylinder through a reheating steam pipeline, the steam outlet of the middle-low pressure cylinder is connected with the steam inlet of a condenser, the condensed water outlet of the condenser is connected with the condensed water inlet of a condensate water tank through a condensed water pipeline, and the condensate water tank is provided with a secondary desalted water inlet;
the outlet of the drum feed water pump is connected with the water inlet of the first drum of the riser, the water outlet of the first drum of the riser is connected with the steam-water mixture inlet of the first drum of the riser through the forced circulation pump and the first riser heat exchanger, the saturated steam outlet of the first drum of the riser is connected with the saturated steam inlet of the second drum of the riser through the second riser heat exchanger, and the superheated steam outlet of the second drum of the riser is connected with a steam pipeline between the high-pressure cylinder and the primary reheater.
The deaerator is a medium-pressure deaerator, and a steam inlet of the deaerator is connected with a low-pressure steam pipe network.
And a reheat steam water spray attemperator is arranged on a connecting pipeline between the primary reheater and the secondary reheater.
And a superheated steam water spraying attemperator is arranged on a connecting pipeline between the primary superheater and the secondary superheater.
The feed water preheater is a radial heat exchange tube type feed water preheater.
The dry quenching boiler is an ultrahigh-temperature ultrahigh-pressure dry quenching boiler, the rated steam temperature is 570 ℃, and the rated steam pressure is 13.7MPa.
The steam turbine generator unit is an ultrahigh-temperature ultrahigh-pressure single-reheat coaxial steam turbine generator unit, the rated steam temperature is 570 ℃, the rated steam pressure is 13.2MPa, the rated steam exhaust temperature of the high-pressure cylinder is 350 ℃, and the rated steam exhaust pressure is 2.8MPa.
The superheated steam outlet of the second steam drum of the rising pipe is additionally connected with a low-pressure steam pipeline through a steam outlet pipeline, and a temperature and pressure reducing device is arranged on the steam outlet pipeline.
A comprehensive utilization method of waste heat in coking production process comprises the following steps:
1) The method comprises the steps of directly feeding externally supplied supplementary secondary desalted water with the temperature of 25-30 ℃ into a desalting water tank, exchanging heat between exhaust steam generated after a low-pressure cylinder in a turbo generator set does work and circulating cooling water through a condenser, feeding the generated condensed water with the temperature of 40-45 ℃ into the desalting water tank through a condensate pump, mixing the condensed water with the supplementary secondary desalted water in the desalting water tank, pressurizing by a deoxidizing water supply pump, feeding the mixture into a water supply preheater, heating the mixture to the water temperature of 60-70 ℃ to enter the deaerator, heating the mixture to the water temperature of more than 120 ℃ and feeding the mixture in two ways, pressurizing by a boiler water supply pump in one way to an economizer in a dry quenching boiler, and pressurizing by a drum water supply pump in the other way to a first drum of an ascending pipe;
2) The boiler water fed to the economizer is subjected to heat exchange by the economizer to enable the water temperature to rise to more than 290 ℃ and enter a boiler steam drum, the saturation temperature of the boiler water in the boiler steam drum is more than 340 ℃, the boiler water enters a membrane water-cooled wall and an evaporator through a down pipe, steam-water mixture is formed after absorbing heat and vaporization and enters the boiler steam drum under the action of hot pressing, saturated steam is generated by separating the steam-water mixture in the boiler steam drum through a steam-water separation device, the saturated steam enters a primary superheater through a collecting pipe and exchanges heat with high-temperature inert circulating gas to enable the steam temperature to rise, after the steam temperature is adjusted to a set temperature through a hot steam water spraying attemperator, the steam enters a secondary superheater and exchanges heat with the high-temperature inert circulating gas to rise, and finally the steam with the final temperature reaching more than 570 ℃ completely enters a high-pressure cylinder in a turbo generator set to generate electricity, the steam of which is more than 350 ℃ after acting, and the high-pressure cylinder steam with the pressure of more than 2.8MPa is discharged to a primary reheater in a dry quenching boiler;
3) The steam drum water fed into the first steam drum of the upper riser is pressurized by a forced circulation pump and fed into a first riser heat exchanger, the generated saturated steam-water mixture enters the first steam drum of the upper riser, the steam-water mixture is separated into saturated steam by a steam-water separation device in the first steam drum of the upper riser, the saturated steam enters a second riser heat exchanger through a collecting pipe, heat exchange is carried out between the saturated steam and high-temperature raw coke oven gas in the second riser heat exchanger, the steam with the temperature of more than 350 ℃ enters the second steam drum of the upper riser, the temperature led out from the second steam drum of the upper riser is more than 350 ℃, the superheated steam with the pressure of more than 2.8MPa is converged with the high-pressure cylinder exhaust steam to form one path, and the path is fed into a primary reheater in a dry quenching boiler;
4) The converged superheated steam exchanges heat with high-temperature inert circulating gas in a primary reheater to enable the temperature of the steam to rise, the reheated steam is sprayed to a attemperator to adjust the temperature of the steam to a set value, then the steam enters a secondary reheater, exchanges heat with the high-temperature inert circulating gas to raise the temperature, and finally the superheated steam with the temperature of more than 570 ℃ completely enters a low-pressure cylinder in a turbo generator set to generate electricity.
When the dry quenching boiler is in an accident overhaul working condition, the superheated steam generated by the second steam drum of the ascending pipe is merged into a low-pressure steam pipe network through a temperature and pressure reducing device and is used by a low-pressure steam user.
Compared with the prior art, the invention has the beneficial effects that:
1) The characteristics of the arrangement of the two existing waste heat recovery systems in the area of a coking enterprise, the waste heat recovery mode, steam parameters and the like are fully considered, the two waste heat recovery systems are organically combined, the problems of waste heat dissipation, high-parameter steam temperature and pressure reduction use and the like are avoided according to the energy utilization principle of 'quality-based energy utilization, temperature opposite and cascade utilization', the maximum improvement of the waste heat utilization rate is realized, the ton coke energy consumption of the enterprise is reduced, and the energy saving and consumption reduction effects are remarkable;
2) The ultra-high temperature and ultra-high pressure unit is adopted to generate electricity, the generating capacity is improved, and the economic benefit is remarkable;
3) The ultra-high temperature and ultra-high pressure dry quenching boiler is adopted, so that the area of a reheater is increased, and the utilization rate of high-grade parameter steam is improved;
4) The dry quenching device and the coke oven riser device are combined and distributed, and share one water supply system, so that the system optimization is realized, the distance between the devices is shortened, and the reduction of the temperature drop and the pressure drop of the superheated steam is facilitated.
Drawings
FIG. 1 is a schematic diagram of a comprehensive utilization system of waste heat in a coking production process.
In the figure, 1, a demineralized water tank 2, a high pressure cylinder 3, a medium low pressure cylinder 4, a condenser 5, a condensate pump 6, a deoxidizing feed pump 7, a feedwater preheater 8, a deaerator 9, a boiler feed pump 10, an economizer 11, a boiler drum 12, a membrane water wall and an evaporator 13, a primary reheater 14, a reheat steam water spray attemperator 15, a secondary reheater 16, a primary superheater 17, a superheated steam water spray attemperator 18, a secondary superheater 19, a generator 20, a riser first drum 21, a forced circulation pump 22, a first riser heat exchanger 23, a second riser heat exchanger 24, a riser second drum 25, a desuperheater 26, and a drum feed pump
Detailed Description
The following is a further description of embodiments of the invention, taken in conjunction with the accompanying drawings:
The invention discloses a comprehensive waste heat utilization system in a coking production process, which comprises a dry quenching waste heat recovery system and a raw gas waste heat recovery system, wherein the dry quenching waste heat recovery system comprises a desalting water tank 1, a turbo generator set and a dry quenching boiler, the turbo generator set comprises a high-pressure cylinder 2, a middle-low pressure cylinder 3 and a generator 19 which are sequentially connected, the dry quenching boiler comprises a boiler steam drum 11, an economizer 10, a membrane water cooler and evaporator 12, a primary reheater 13, a secondary reheater 15, a primary superheater 16 and a secondary superheater 18 which are sequentially arranged in the dry quenching boiler body from bottom to top, the raw gas waste heat recovery system comprises a first riser steam drum 20, a first riser heat exchanger 22, a second riser steam drum 24 and a second riser heat exchanger 23, and the comprehensive utilization system comprises the following specific structures:
The system comprises a demineralized water tank 1, a demineralized water feed pump 6, a water feed preheater 7 and a deaerator 8, wherein the demineralized water outlet of the demineralized water tank 1 is sequentially connected with the deaeration feed pump 6, the water feed preheater 7 and the deaerator 8 through a demineralized water outlet pipeline, the water feed preheater 7 is arranged at a circulating gas outlet of a dry quenching boiler, the deaerated water outlet of the deaerator 8 is respectively connected with an inlet of a boiler feed pump 9 and an inlet of a steam drum feed pump 26, an outlet of the boiler feed pump 9 is connected with a water inlet of an economizer 10 in the dry quenching boiler, a water outlet of the economizer 10 is connected with a water inlet of a boiler steam drum 11, a water outlet of the boiler steam drum 11 is connected with a steam-water mixture inlet of the boiler steam drum 11 through a membrane water cooler and an evaporator 12, a saturated steam outlet of the boiler steam drum 11 is sequentially connected with a steam inlet of a high-pressure cylinder 2 in the steam turbine generator set through a primary superheater 16 and a secondary superheater 18, the steam outlet of the high-pressure cylinder 2 is connected with a primary reheater 13 and a secondary reheater 15 through a reheat steam pipeline, the secondary reheater 15 is connected with a steam inlet of a low-pressure cylinder 3, the steam outlet of the low-pressure cylinder 3 is connected with a steam inlet of a condenser 4, a water outlet of the condenser 4 is connected with a water inlet of the condensate 1 through a pipeline, and a condensate water tank 1 is provided with a condensate water pump 1;
the outlet of the steam drum water supply pump 26 is connected with the water inlet of the first steam drum 20 of the rising pipe, the water outlet of the first steam drum 20 of the rising pipe is connected with the steam-water mixture inlet of the first steam drum 20 of the rising pipe through the forced circulation pump 21 and the first rising pipe heat exchanger 22, the saturated steam outlet of the first steam drum 20 of the rising pipe is connected with the saturated steam inlet of the second steam drum 24 of the rising pipe through the second rising pipe heat exchanger 23, and the superheated steam outlet of the second steam drum 24 of the rising pipe is connected with a steam pipeline between the high-pressure cylinder 2 and the primary reheater 13.
The deaerator 8 is a medium-pressure deaerator, and the deaerator 8 is provided with a steam inlet connected with a low-pressure steam pipe network.
A reheat steam water spray attemperator 14 is arranged on a connecting pipeline between the primary reheater 13 and the secondary reheater 15.
And a superheated steam water spray attemperator 17 is arranged on a connecting pipeline between the primary superheater 16 and the secondary superheater 18.
The feed water preheater 7 is a radial heat exchange tube type feed water preheater.
The dry quenching boiler is an ultrahigh-temperature ultrahigh-pressure dry quenching boiler, the rated steam temperature is 570 ℃, and the rated steam pressure is 13.7MPa.
The steam turbine generator unit is an ultrahigh-temperature ultrahigh-pressure single-reheat coaxial steam turbine generator unit, the rated steam temperature is 570 ℃, the rated steam pressure is 13.2MPa, the rated steam exhaust temperature of the high-pressure cylinder is 350 ℃, and the rated steam exhaust pressure is 2.8MPa.
The superheated steam outlet of the second steam drum 24 of the rising pipe is additionally connected with a low-pressure steam pipeline through a steam outlet pipeline, and a temperature and pressure reducing device 25 is arranged on the steam outlet pipeline.
The working principle of the waste heat comprehensive utilization system in the coking production process is that desalted water is sent to a deaerator 8 after heat exchange by a water supply preheater 7, deaerated water with the temperature of 120 ℃ after deaeration is divided into two paths, one path is boiler water supply, superheated steam with the temperature of 570 ℃ and the pressure of 13.7MPa is generated by a dry quenching boiler and is sent to a high-pressure cylinder 2 of a steam turbine generator unit to generate electricity, the other path is drum water supply, saturated steam with the temperature of 236 ℃ and the pressure of 3.0MPa is generated by a first riser heat exchanger 22, the saturated steam generates superheated steam with the temperature of 350 ℃ and the pressure of 2.8MPa by a second riser heat exchanger 23, and the superheated steam with the temperature of 350 ℃ and the pressure of 2.8MPa in the steam turbine generator unit is discharged and is converged into one path into a primary reheater 13 and a secondary reheater 15 of the dry quenching boiler, and the superheated steam with the temperature of 570 ℃ and the pressure of 2.5MPa after reheating enters a middle-low-pressure cylinder 3 of the steam turbine generator unit to generate electricity.
The first riser tube heat exchanger 22 and the second riser tube heat exchanger 23 are arranged on the coke oven riser tube, and are all a plurality of.
A comprehensive utilization method of waste heat in coking production process comprises the following steps:
1) The externally supplied secondary desalting water with the temperature of 25-30 ℃ directly enters a desalting water tank 1, waste steam generated by a low-pressure cylinder 3 in a turbo generator set after working is subjected to heat exchange with circulating cooling water through a condenser, the generated condensed water with the temperature of 40-45 ℃ enters the desalting water tank 1 through a condensate pump 4, is mixed with the secondary desalting water in the desalting water tank 1, is pressurized by a deoxidizing water supply pump 6 and is sent to a water supply preheater 7, the heated water temperature is increased to 60-70 ℃ and enters a deaerator 8, the heated water temperature is increased to 120 ℃ and is sent out in two ways, wherein one of the two ways is pressurized by a boiler water supply pump 9 and is sent to an economizer 10 in a dry quenching boiler, and the other way is pressurized by a steam drum water supply pump 26 and is sent to a first steam drum 20 of an ascending pipe;
2) The boiler water fed to the economizer 10 is subjected to heat exchange by the economizer 10 to enable the water temperature to rise to more than 290 ℃ and enter a boiler steam drum 11, the saturation temperature of the boiler water in the boiler steam drum 11 is more than 340 ℃, the boiler water enters a membrane water-cooled wall and an evaporator 12 from a down pipe, steam-water mixture is formed after absorbing heat and vaporization and enters the boiler steam drum 11 under the action of hot pressing, the steam-water mixture is separated in the boiler steam drum 11 through a steam-water separation device to generate saturated steam, the saturated steam enters a primary superheater 116 through a collecting pipe, the primary superheater 16 is subjected to heat exchange with high-temperature inert circulating gas to enable the steam temperature to rise, the steam enters a secondary superheater 18 to be subjected to heat exchange with the high-temperature inert circulating gas to rise after the steam temperature is adjusted to be higher than 570 ℃, and the steam with the final temperature reaching more than 570 ℃ is completely fed into a high-pressure cylinder 2 in a turbo generator set to generate electricity, and the high-pressure cylinder 2 with the temperature being more than 350 ℃ after the steam is discharged to the steam to be sent to a primary reheater 13 in a dry quenching boiler;
3) The steam drum water fed to the first riser pipe steam drum 20 is pressurized by a forced circulation pump 21 and fed to a first riser pipe heat exchanger 22, the generated saturated steam-water mixture enters the first riser pipe steam drum 20, the steam-water mixture is separated in the first riser pipe steam drum 20 by a steam-water separation device to generate saturated steam, the saturated steam enters a second riser pipe heat exchanger 23 through a collecting pipe, heat exchange is carried out between the saturated steam and high-temperature raw coke oven gas in the second riser pipe heat exchanger 23, the steam with the temperature of more than 350 ℃ enters a second riser pipe steam drum 24, the temperature led out from the second riser pipe steam drum 24 is more than 350 ℃, and the superheated steam with the pressure of more than 2.8MPa is converged with the steam discharged from the high-pressure cylinder 2 to form one path, and the saturated steam is fed to a primary reheater 13 in a dry quenching boiler;
4) The converged superheated steam exchanges heat with the high-temperature inert circulating gas in the primary reheater 13 to raise the steam temperature, the steam temperature is adjusted to a set value through the reheated steam water spraying attemperator 14 and then enters the secondary reheater 15, the superheated steam exchanges heat with the high-temperature inert circulating gas to raise the temperature, and the superheated steam with the final temperature of more than 570 ℃ completely enters the low-pressure cylinder 3 in the turbo generator set to generate power.
When the dry quenching boiler is in an accident overhaul working condition, the superheated steam generated by the second steam drum 24 of the ascending pipe is merged into a low-pressure steam pipe network through the temperature and pressure reducing device 25 for a low-pressure steam user to use.
The foregoing is only a preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art, who is within the scope of the present invention, should make equivalent substitutions or modifications according to the technical scheme of the present invention and the inventive concept thereof, and should be covered by the scope of the present invention.
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| CN114017767A (en) * | 2021-11-25 | 2022-02-08 | 苏州克兰茨环境科技有限公司 | A system for improving the grade of low-grade steam by using waste gas treatment waste heat |
| CN114719237B (en) * | 2022-04-28 | 2024-04-23 | 中冶焦耐(大连)工程技术有限公司 | Multi-stage temperature reduction technology for power generation by using ultrahigh temperature, ultrahigh pressure and dry quenching waste heat |
| CN114774137A (en) * | 2022-04-29 | 2022-07-22 | 中冶焦耐(大连)工程技术有限公司 | Coke oven riser waste heat steam production heating reheating method and system |
| CN115406252B (en) * | 2022-08-11 | 2024-05-24 | 中材节能股份有限公司 | A comprehensive utilization method of cement kiln waste heat based on single reheating technology |
| CN115418240B (en) * | 2022-08-22 | 2025-01-10 | 中冶焦耐(大连)工程技术有限公司 | Comprehensive water supply and dosing system and method for coking waste heat utilization under full dry quenching mode |
| CN115523481A (en) * | 2022-09-29 | 2022-12-27 | 中冶焦耐(大连)工程技术有限公司 | Method and system for utilizing surplus steam of coking enterprise |
| CN116379791A (en) * | 2023-04-26 | 2023-07-04 | 武钢集团昆明钢铁股份有限公司 | Heat exchange process and heat exchange system for recycling waste heat of boiler flue gas |
| CN117232274A (en) * | 2023-09-14 | 2023-12-15 | 北京首钢国际工程技术有限公司 | Waste heat recovery device for dry dedusting of converter gas |
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