CN215261220U - Comprehensive utilization system for waste heat in coking production process - Google Patents
Comprehensive utilization system for waste heat in coking production process Download PDFInfo
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Abstract
The utility model relates to a comprehensive utilization system for waste heat in the coking production process, which comprises a dry quenching waste heat recovery system and a raw coke oven gas waste heat recovery system; the dry quenching waste heat recovery system comprises a desalting water tank, a steam turbine generator unit and a dry quenching boiler; the steam turbine generator unit 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 arranged in the dry quenching boiler body in sequence from bottom to top; the raw gas waste heat recovery system comprises a first steam drum of an ascending pipe, a first ascending pipe heat exchanger, a second steam drum of the ascending pipe and a second ascending pipe heat exchanger; the utility model can improve the coking waste heat utilization rate to the maximum extent and reduce the ton coke energy consumption of enterprises; meanwhile, the ultra-high temperature and ultra-high pressure unit is adopted to generate electricity, so that the generated energy is improved, and the economic benefit and the energy-saving and consumption-reducing effects are obvious.
Description
Technical Field
The utility model relates to a coking production waste heat recovery technical field especially relates to a coking production process waste heat comprehensive utilization system.
Background
At present, the waste heat recovery measures generally adopted by coking enterprises comprise raw coke oven gas waste heat recovery and red coke waste heat recovery, wherein the raw coke oven gas waste heat recovery is to utilize a coke oven riser to exchange heat to generate low-pressure saturated steam for low-pressure steam users, the red coke waste heat recovery is to utilize a dry quenching boiler to generate high-temperature high-pressure superheated steam for a steam turbine generator set to generate electricity, and the raw coke oven gas waste heat recovery and the red coke waste heat recovery are relatively independent.
The method further accelerates the transformation and upgrading of the coking industry, promotes the technical progress of the coking industry, improves the comprehensive utilization rate of resources and the energy-saving and environment-friendly level, and promotes the high-quality development of the coking industry. The utility model discloses combine two production technology systems of raw coke oven gas waste heat recovery and red burnt waste heat recovery organically, according to the waste heat utilization characteristics and the waste heat steam parameter of every process system, according to the energy utilization principle of "utilize according to matter ability, temperature to mouthful, step" avoid waste heat to diffuse, the emergence that the high parameter steam temperature reduction decompressed and used the scheduling problem, furthest's improvement waste heat utilization rate reduces the burnt energy consumption of enterprise ton.
Disclosure of Invention
The utility model provides a waste heat comprehensive utilization system in the coking production process, which can improve the coking waste heat utilization rate to the maximum extent and reduce the energy consumption of the coke per ton of enterprises; meanwhile, the ultra-high temperature and ultra-high pressure unit is adopted to generate electricity, so that the generated energy is improved, and the economic benefit and the energy-saving and consumption-reducing effects are obvious.
In order to achieve the above purpose, the utility model adopts the following technical scheme:
a comprehensive utilization system for waste heat in a coking production process comprises a dry quenching waste heat recovery system; the system also comprises a raw gas waste heat recovery system; the dry quenching waste heat recovery system comprises a desalting water tank, a steam turbine generator unit and a dry quenching boiler; the steam turbine generator unit 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 arranged in the dry quenching boiler body in sequence from bottom to top; the raw coke oven gas waste heat recovery system comprises a first steam drum of an ascending pipe, a first ascending pipe heat exchanger, a second steam drum of the ascending pipe and a second ascending pipe heat exchanger; the concrete structure is as follows:
a demineralized water outlet of the demineralized water tank is sequentially connected with a deoxidizing water feeding pump, a water feeding preheater and a deaerator through a demineralized water outlet pipeline, wherein the water feeding preheater is arranged at a circulating gas outlet of the dry quenching boiler; a deaerated water outlet of the deaerator is respectively connected with an inlet of a boiler feed water pump and an inlet of a steam pocket feed water pump; the outlet of the boiler feed water pump is connected with the water inlet of an economizer in the dry coke quenching boiler; the water outlet of the economizer is connected with the water inlet of a boiler drum, the water outlet of the boiler drum is connected with a steam-water mixture inlet of the boiler drum through a membrane water cooler and an evaporator, and a saturated steam outlet of the boiler drum is connected with a steam inlet of a high-pressure cylinder in a steam turbine generator unit through a primary superheater and a secondary superheater in sequence; a steam outlet of the high-pressure cylinder is connected with a primary reheater and a secondary reheater through a steam pipeline, and the secondary reheater is connected with a steam inlet of the medium-low pressure cylinder through a reheat steam pipeline; a steam outlet of the medium-low pressure cylinder is connected with a steam inlet of a condenser, a condensed water outlet of the condenser is connected with a condensed water inlet of the desalting water tank through a condensed water pipeline, and a condensed water pump is arranged on the condensed water pipeline; the desalting water tank is also provided with a secondary desalting water inlet;
the outlet of the steam drum water supply pump is connected with the water inlet of a first steam drum of the ascending pipe, the water outlet of the first steam drum of the ascending pipe is connected with the steam-water mixture inlet of the first steam drum of the ascending pipe through the forced circulation pump and the first ascending pipe heat exchanger, the saturated steam outlet of the first steam drum of the ascending pipe is connected with the saturated steam inlet of a second steam drum of the ascending pipe through the second ascending pipe heat exchanger, and the superheated steam outlet of the second steam drum of the ascending pipe is connected with the 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 desuperheater is arranged on a connecting pipeline between the primary reheater and the secondary reheater.
And a superheated steam water spraying desuperheater 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 13.7 MPa.
The steam turbine generator unit is an ultrahigh-temperature ultrahigh-pressure belt single-reheating coaxial steam turbine generator unit, the rated steam temperature is 570 ℃, the rated steam pressure is 13.2MPa, the rated exhaust steam temperature of the high-pressure cylinder is 350 ℃, and the rated exhaust steam pressure is 2.8 MPa.
The superheated steam outlet of the second steam drum of the ascending 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.
Compared with the prior art, the beneficial effects of the utility model are that:
1) the characteristics of the two existing waste heat recovery systems in regional arrangement, waste heat recovery modes, steam parameters and the like of a coking enterprise are fully considered, the two waste heat recovery systems are organically combined, and the problems of waste heat diffusion, high-parameter steam temperature and pressure reduction use and the like are avoided according to the energy utilization principle of 'utilization according to quality energy, temperature and gradient utilization', so that the waste heat utilization rate is improved to the maximum extent, the energy consumption of the enterprise per ton coke is reduced, and the energy saving and consumption reducing effects are obvious;
2) the ultra-high temperature and ultra-high pressure unit is adopted for power generation, so that the generated energy is improved, and the economic benefit is remarkable;
3) an ultrahigh-temperature and ultrahigh-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 ascending pipe device are jointly distributed and share one set of water supply system, so that system optimization is realized; the distance between the devices is shortened, and the temperature drop and the pressure drop of the superheated steam are reduced.
Drawings
FIG. 1 is a schematic structural diagram of a system for comprehensively utilizing waste heat in a coking production process.
In the figure: 1. desalting water tank 2, high-pressure cylinder 3, medium-low pressure cylinder 4, condenser 5, condensate pump 6, deoxidizing water-feeding pump 7, water-feeding preheater 8, deaerator 9, boiler water-feeding pump 10, economizer 11, boiler drum 12, membrane water-cooling wall and evaporator 13, primary reheater 14, reheated steam water-spraying desuperheater 15, secondary reheater 16, primary superheater 17, superheated steam water-spraying desuperheater 18, secondary superheater 19, generator 20, riser first drum 21, forced circulation pump 22, first riser heat exchanger 23, second riser heat exchanger 24, riser second drum 25, desuperheating pressure reducing 26, drum water-feeding pump
Detailed Description
The following description of the embodiments of the present invention will be made with reference to the accompanying drawings:
as shown in figure 1, the waste heat comprehensive utilization system in the coking production process comprises a dry quenching waste heat recovery system; the system also comprises a raw gas waste heat recovery system; the dry quenching waste heat recovery system comprises a demineralized water tank 1, a turbo generator set and a dry quenching boiler; the steam turbine generator unit comprises a high-pressure cylinder 2, a medium-low pressure cylinder 3 and a generator 19 which are connected in sequence; the dry quenching boiler comprises a boiler steam drum 11, and 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 arranged in the dry quenching boiler body in sequence from bottom to top; the raw coke oven gas waste heat recovery system comprises a first ascending pipe steam drum 20, a first ascending pipe heat exchanger 22, a second ascending pipe steam drum 24 and a second ascending pipe heat exchanger 23; the concrete structure is as follows:
a demineralized water outlet of the demineralized water tank 1 is sequentially connected with a deoxygenation water feed pump 6, a water feed preheater 7 and a deoxygenator 8 through a demineralized water outlet pipeline, wherein the water feed preheater 7 is arranged at a circulating gas outlet of the dry quenching boiler; a deoxygenated water outlet of the deoxygenator 8 is respectively connected with an inlet of a boiler feed water pump 9 and an inlet of a steam pocket feed water pump 26; the outlet of the boiler water feed pump 9 is connected with the water inlet of an economizer 10 in the dry coke quenching boiler; the water outlet of the economizer 10 is connected with the water inlet of a boiler drum 11, the water outlet of the boiler drum 11 is connected with the steam-water mixture inlet of the boiler drum 11 through a membrane water cooler and an evaporator 12, and the saturated steam outlet of the boiler drum 11 is connected with the steam inlet of a high pressure cylinder 2 in the steam turbine generator unit sequentially through a primary superheater 16 and a secondary superheater 18; a steam outlet of the high-pressure cylinder 2 is connected with a primary reheater 13 and a secondary reheater 15 through steam pipelines, and the secondary reheater 15 is connected with a steam inlet of the medium-low pressure cylinder 3 through a reheating steam pipeline; a steam outlet of the medium and low pressure cylinder 3 is connected with a steam inlet of a condenser 4, a condensed water outlet of the condenser 4 is connected with a condensed water inlet of the desalted water tank 1 through a condensed water pipeline, and a condensed water pump 5 is arranged on the condensed water pipeline; the demineralized water tank 1 is also provided with a secondary demineralized water inlet;
an outlet of the steam pocket water feeding pump 26 is connected with a water inlet of a first steam pocket 20 of the ascending pipe, a water outlet of the first steam pocket 20 of the ascending pipe is connected with a steam-water mixture inlet of the first steam pocket 20 of the ascending pipe through a forced circulation pump 21 and a first ascending pipe heat exchanger 22, a saturated steam outlet of the first steam pocket 20 of the ascending pipe is connected with a saturated steam inlet of a second steam pocket 24 of the ascending pipe through a second ascending pipe heat exchanger 23, and a superheated steam outlet of the second steam pocket 24 of the ascending 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.
And a reheat steam water spray desuperheater 14 is arranged on a connecting pipeline between the primary reheater 13 and the secondary reheater 15.
And a connecting pipeline between the primary superheater 16 and the secondary superheater 18 is provided with a superheated steam water spraying desuperheater 17.
The feed water preheater 7 is a radial heat exchange tube 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 13.7 MPa.
The steam turbine generator unit is an ultrahigh-temperature ultrahigh-pressure belt single-reheating coaxial steam turbine generator unit, the rated steam temperature is 570 ℃, the rated steam pressure is 13.2MPa, the rated exhaust steam temperature of the high-pressure cylinder is 350 ℃, and the rated exhaust steam pressure is 2.8 MPa.
The superheated steam outlet of the second steam pocket 24 of the ascending 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 as follows: the desalted water is sent to a deaerator 8 after heat exchange through a feed water preheater 7, deaerated water with the temperature of 120 ℃ is divided into two paths, one path is boiler feed water, and superheated steam with the temperature of about 570 ℃ and the pressure of about 13.7MPa is generated by a dry quenching boiler and sent to a high-pressure cylinder 2 of a turbo generator set for power generation; one path is steam drum feed water, saturated steam with the temperature of about 236 ℃ and the pressure of about 3.0MPa is generated by the first ascending pipe heat exchanger 22, the saturated steam generates superheated steam with the temperature of about 350 ℃ and the pressure of about 2.8MPa by the second ascending pipe heat exchanger 23, and the superheated steam is merged with exhaust steam of a high pressure cylinder 2 in the steam turbine generator unit with the temperature of about 350 ℃ and the pressure of about 2.8MPa to form a path, and the path enters a primary reheater 13 and a secondary reheater 15 of the dry quenching boiler for reheating, and the superheated steam with the temperature of about 570 ℃ and the pressure of about 2.5MPa enters a low pressure cylinder 3 of the steam turbine generator unit for power generation.
The first rising pipe heat exchanger 22 and the second rising pipe heat exchanger 23 are arranged on the rising pipe of the coke oven and are respectively provided with a plurality of rising pipes.
The process method of the waste heat comprehensive utilization system in the coking production process comprises the following steps:
1) supplying supplementary secondary desalted water with the temperature of 25-30 ℃ which is supplied from the outside, directly entering a desalted water tank 1, exchanging heat between exhaust steam which is used for doing work and circulating cooling water in a low-pressure cylinder 3 in a steam turbine generator unit through a condenser, and then leading the generated condensed water with the temperature of 40-45 ℃ to enter the desalted water tank 1 through a condensed water pump 4, mixing the condensed water with the supplementary secondary desalted water in the desalted water tank 1, then pressurizing and sending the condensed water to a feed water preheater 7 through a deoxygenation feed water pump 6, heating the water to 60-70 ℃, entering a deoxygenator 8, heating the water to 120 ℃ and sending the heated water out in two paths; one path is pressurized and sent to an economizer 10 in the dry coke quenching boiler by a boiler water feed pump 9, and the other path is pressurized and sent to a first steam pocket 20 of the ascending pipe by a steam pocket water feed pump 26;
2) the boiler feed water sent to the economizer 10 is subjected to heat exchange through the economizer 10 to enable the water temperature to rise to more than 290 ℃ and enter the 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 the membrane water wall and the evaporator 12 through a downcomer, a steam-water mixture is formed after heat absorption and vaporization and enters the boiler steam drum 11 under the action of hot pressing, the steam-water mixture is separated by a steam-water separation device in the boiler steam drum 11 to generate saturated steam, and the saturated steam enters the primary superheater 116 through a confluence pipe; exchanging heat with the high-temperature inert circulating gas in the primary superheater 16 to raise the temperature of the steam; after the temperature of the steam is adjusted to a set temperature by a superheated steam water spray desuperheater 17, the steam enters a secondary superheater 18 to exchange heat with high-temperature inert circulating gas to raise the temperature, the steam with the final temperature of more than 570 ℃ completely enters a high-pressure cylinder 2 in a turbo generator set to generate power, and the exhausted steam of the high-pressure cylinder 2 with the temperature of more than 350 ℃ and the pressure of more than 2.8MPa after acting is sent to a primary reheater 13 in a dry coke quenching boiler;
3) the steam pocket feed water sent to the first steam pocket 20 of the ascending pipe is pressurized and sent to a first ascending pipe heat exchanger 22 through a forced circulation pump 21, the generated saturated steam-water mixture enters the first steam pocket 20 of the ascending pipe, the steam-water mixture is separated by a steam-water separation device in the first steam pocket 20 of the ascending pipe to generate saturated steam, and the saturated steam enters a second ascending pipe heat exchanger 23 through a collecting pipe; exchanging heat with high-temperature raw coke gas in a second riser heat exchanger 23, introducing steam with the temperature increased to more than 350 ℃ into a second steam pocket 24 of the riser, leading out superheated steam with the temperature of more than 350 ℃ and the pressure of more than 2.8MPa from the second steam pocket 24 of the riser, combining the superheated steam with the exhaust steam of the high-pressure cylinder 2 into a path, and sending the path to a primary reheater 13 in a dry coke quenching boiler;
4) the merged superheated steam exchanges heat with high-temperature inert circulating gas in a primary reheater 13 to raise the temperature of the steam, the steam temperature is adjusted to a set value through a reheated steam water spray desuperheater 14 and then enters a secondary reheater 15 to exchange 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 3 in a steam turbine generator unit to generate power.
When the dry quenching boiler is in the accident maintenance working condition, superheated steam generated by the second steam pocket 24 of the ascending pipe is merged into a low-pressure steam pipe network through the temperature and pressure reducing device 25 for low-pressure steam users to use.
The above, only be the concrete implementation of the preferred embodiment of the present invention, but the protection scope of the present invention is not limited thereto, and any person skilled in the art is in the technical scope of the present invention, according to the technical solution of the present invention and the utility model, the concept of which is equivalent to replace or change, should be covered within the protection scope of the present invention.
Claims (8)
1. A comprehensive utilization system for waste heat in a coking production process comprises a dry quenching waste heat recovery system; the system is characterized by also comprising a raw gas waste heat recovery system; the dry quenching waste heat recovery system comprises a desalting water tank, a steam turbine generator unit and a dry quenching boiler; the steam turbine generator unit 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 arranged in the dry quenching boiler body in sequence from bottom to top; the raw coke oven gas waste heat recovery system comprises a first steam drum of an ascending pipe, a first ascending pipe heat exchanger, a second steam drum of the ascending pipe and a second ascending pipe heat exchanger; the concrete structure is as follows:
a demineralized water outlet of the demineralized water tank is sequentially connected with a deoxidizing water feeding pump, a water feeding preheater and a deaerator through a demineralized water outlet pipeline, wherein the water feeding preheater is arranged at a circulating gas outlet of the dry quenching boiler; a deaerated water outlet of the deaerator is respectively connected with an inlet of a boiler feed water pump and an inlet of a steam pocket feed water pump; the outlet of the boiler feed water pump is connected with the water inlet of an economizer in the dry coke quenching boiler; the water outlet of the economizer is connected with the water inlet of a boiler drum, the water outlet of the boiler drum is connected with a steam-water mixture inlet of the boiler drum through a membrane water cooler and an evaporator, and a saturated steam outlet of the boiler drum is connected with a steam inlet of a high-pressure cylinder in a steam turbine generator unit through a primary superheater and a secondary superheater in sequence; a steam outlet of the high-pressure cylinder is connected with a primary reheater and a secondary reheater through a steam pipeline, and the secondary reheater is connected with a steam inlet of the medium-low pressure cylinder through a reheat steam pipeline; a steam outlet of the medium-low pressure cylinder is connected with a steam inlet of a condenser, a condensed water outlet of the condenser is connected with a condensed water inlet of the desalting water tank through a condensed water pipeline, and a condensed water pump is arranged on the condensed water pipeline; the desalting water tank is also provided with a secondary desalting water inlet;
the outlet of the steam drum water supply pump is connected with the water inlet of a first steam drum of the ascending pipe, the water outlet of the first steam drum of the ascending pipe is connected with the steam-water mixture inlet of the first steam drum of the ascending pipe through the forced circulation pump and the first ascending pipe heat exchanger, the saturated steam outlet of the first steam drum of the ascending pipe is connected with the saturated steam inlet of a second steam drum of the ascending pipe through the second ascending pipe heat exchanger, and the superheated steam outlet of the second steam drum of the ascending pipe is connected with the steam pipeline between the high-pressure cylinder and the primary reheater.
2. The comprehensive utilization system of the waste heat in the coking production process according to claim 1, characterized in that the deaerator is a medium-pressure deaerator, and the deaerator is provided with a steam inlet connected with a low-pressure steam pipe network.
3. The comprehensive utilization system of the waste heat in the coking production process according to claim 1, characterized in that a reheat steam water spray desuperheater is arranged on a connecting pipeline between the primary reheater and the secondary reheater.
4. The comprehensive utilization system of the waste heat in the coking production process according to claim 1, characterized in that a superheated steam water spray desuperheater is arranged on a connecting pipeline between the primary superheater and the secondary superheater.
5. The comprehensive utilization system of waste heat in a coking production process according to claim 1, characterized in that the feed water preheater is a radial heat exchange tube type feed water preheater.
6. The comprehensive utilization system of the waste heat in the coking production process according to claim 1, characterized in that the dry quenching boiler is an ultrahigh temperature and ultrahigh pressure dry quenching boiler, the rated steam temperature is 570 ℃, and the rated steam pressure is 13.7 MPa.
7. The comprehensive utilization system of the waste heat in the coking production process according to claim 1, characterized in that the steam turbine generator unit is an ultrahigh temperature and ultrahigh pressure belt single reheating coaxial steam turbine generator unit, the rated steam temperature is 570 ℃, the rated steam pressure is 13.2MPa, the rated exhaust steam temperature of the high pressure cylinder is 350 ℃, and the rated exhaust steam pressure is 2.8 MPa.
8. The comprehensive utilization system of the waste heat in the coking production process according to claim 1, wherein the superheated steam outlet of the second steam pocket of the riser 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.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113446863A (en) * | 2021-05-20 | 2021-09-28 | 中冶焦耐(大连)工程技术有限公司 | Comprehensive utilization system and method for waste heat in coking production process |
| CN115418240A (en) * | 2022-08-22 | 2022-12-02 | 中冶焦耐(大连)工程技术有限公司 | Comprehensive water and chemical feeding system and method for coking waste heat utilization in full dry quenching mode |
| CN117213250A (en) * | 2023-08-22 | 2023-12-12 | 鞍钢股份有限公司 | Coke oven riser waste heat high-quality utilization device and method |
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2021
- 2021-05-20 CN CN202121086769.1U patent/CN215261220U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113446863A (en) * | 2021-05-20 | 2021-09-28 | 中冶焦耐(大连)工程技术有限公司 | Comprehensive utilization system and method for waste heat in coking production process |
| CN115418240A (en) * | 2022-08-22 | 2022-12-02 | 中冶焦耐(大连)工程技术有限公司 | Comprehensive water and chemical feeding system and method for coking waste heat utilization in full dry quenching mode |
| CN117213250A (en) * | 2023-08-22 | 2023-12-12 | 鞍钢股份有限公司 | Coke oven riser waste heat high-quality utilization device and method |
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