CN214536093U - Low-grade waste heat recovery system of coking production system - Google Patents
Low-grade waste heat recovery system of coking production system Download PDFInfo
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- CN214536093U CN214536093U CN202023293473.5U CN202023293473U CN214536093U CN 214536093 U CN214536093 U CN 214536093U CN 202023293473 U CN202023293473 U CN 202023293473U CN 214536093 U CN214536093 U CN 214536093U
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Abstract
The utility model relates to a low-grade waste heat recovery system of a coking production system, the coking production system comprises a dry quenching boiler, a steam extraction and condensing steam turbine, a condenser, a condensing water pump, a generator, a crude benzene distillation unit, a deaerator, a deoxidizing water pump, a desalting water tank, a desalting water station, a boiler water pump, a continuous blowdown expander, a blowdown pump and a dry quenching device water seal tank; the low-grade waste heat recovery system comprises a primary water-water heat exchanger and a secondary water-water heat exchanger. The utility model discloses can effectively retrieve crude benzene distillation unit condensate water, flash steam in the coking production process, the continuous low-grade waste heat such as blow off water, secondary steam of dry quenching boiler, the system composition is simple, operation control is convenient.
Description
Technical Field
The utility model relates to a waste heat recovery technical field especially relates to a recovery system of crude benzol distillation unit condensate water, flash steam, low-grade waste heat such as dry coke quenching boiler continuous blow off water, secondary steam among coking production system.
Background
China requires that the utilization rate of the low-grade waste heat reaches 80 percent before 2020. A large amount of low-temperature waste heat can be generated in the coking production process, at present, the large amount of low-temperature waste heat is still not recycled and is discharged to the environment in various forms, so that the environmental pollution is caused, the great waste of low-temperature waste heat resources is caused, and the energy consumption of enterprises is increased.
To low temperature waste heat quality low in the coking production process, retrieve the degree of difficulty big, can recycle the way less than the scheduling problem, the utility model discloses a flash distillation optimal utilization and the method that the peer utilization of condensate water combined together retrieves low-grade waste heat, improve the economic benefits of enterprise conscientiously, have important meaning to the focusing enterprise implementation "reduce cost and improve effect, energy saving and emission reduction".
Disclosure of Invention
The utility model provides a coking production system's low-grade waste heat recovery system can effectively retrieve crude benzene distillation unit condensate water, flash distillation vapour in the coking production process, and the continuous low-grade waste heat such as blow off water, secondary steam of dry quenching boiler, and the system composition is simple, and operation control is convenient.
In order to achieve the above purpose, the utility model adopts the following technical scheme:
a low-grade waste heat recovery system of a coking production system comprises a dry quenching boiler, a steam extraction and condensing steam turbine, a condenser, a condensing water pump, a generator, a crude benzene distillation unit, a deaerator, a deaerating water feed pump, a desalting water tank, a desalting water station, a boiler water feed pump, a continuous blowdown expander, a blowdown pump and a dry quenching device water seal tank; the top of the dry quenching boiler is provided with an inert circulating gas inlet, the bottom of the dry quenching boiler is provided with an inert circulating gas outlet, and the inert circulating gas outlet is provided with a feed water preheater; the dry coke quenching boiler is internally provided with an economizer, a membrane water wall, an evaporator, a primary superheater and a secondary superheater from bottom to top in sequence, the primary superheater and the secondary superheater are connected through a water-spraying type desuperheater, and the economizer, the membrane water wall, the evaporator and the primary superheater are respectively connected with a steam drum; the steam pocket is provided with a continuous blowdown expander; the low-grade waste heat recovery system comprises a primary water-water heat exchanger and a secondary water-water heat exchanger; the desalting water tank is provided with a secondary desalting water inlet, a condensed water inlet and a boiler water supply outlet; the boiler water supply outlet is sequentially connected with a deoxidizing water supply pump, a water supply preheater, a primary water-water heat exchanger, a secondary water-water heat exchanger, a deaerator, a boiler water supply pump, an economizer and a steam drum through a boiler water supply pipeline; the steam pocket is respectively connected with a boiler water supply inlet of the membrane water-cooling wall and a boiler water supply inlet of the evaporator through a downcomer, and a steam-water mixture outlet of the membrane water-cooling wall and a steam-water mixture outlet of the evaporator are respectively connected with a steam-water mixture inlet of a steam-water separation device in the steam pocket; a saturated steam outlet of the steam-water separation device is connected with a steam inlet of a primary superheater through a collecting pipe, an overheated steam outlet of the primary superheater is connected with a steam inlet of a water spray desuperheater, a steam outlet of the water spray desuperheater is connected with a steam inlet of a secondary superheater, and an overheated steam outlet of the secondary superheater is connected with an overheated steam inlet of a steam extraction condensing steam turbine; a superheated steam outlet of the steam extraction condensing steam turbine is connected with a steam inlet of the crude benzene distillation unit; the waste steam outlet of the steam extraction and condensation type steam turbine is sequentially connected with a condenser, a condensate pump and a condensate inlet of a desalting water tank through a condensate water pipeline; a condensed water outlet of the crude benzene distillation unit is sequentially connected with a secondary water-water heat exchanger and a desalted water station through a condensed water pipeline; the continuous blowdown expander is sequentially connected with the primary water-water heat exchanger, the blowdown pump and the water seal tank of the dry quenching device through a blowdown pipeline.
The feed water preheater is a radial heat exchange tube type feed water preheater.
The sewage pump is a long-shaft submerged sewage pump.
The primary water-water heat exchanger and the secondary water-water heat exchanger are both shell-and-tube heat exchangers.
Compared with the prior art, the beneficial effects of the utility model are that:
1) the utility model formulates different waste heat recovery modes according to the characteristics of different low-grade waste heat in the coking production process, accords with the energy utilization principle of 'energy utilization according to quality, temperature and cascade utilization', solves the problems of steam emission, condensed water discharge, waste of waste heat energy and the like, and effectively improves the waste heat utilization rate;
2) compared with other low-grade waste heat recovery systems in the coking production process, the utility model realizes complete low-grade waste heat recovery, can indirectly convert low-grade steam waste heat and condensed water waste heat into high-grade electric energy and steam, and has the advantages of energy conservation and emission reduction;
3) compare with other coking production process low-grade waste heat recovery systems, the utility model discloses a deoxidization return water is earlier through one-level water heat exchanger and the heat transfer of dry coke quenching boiler blow-down water, and the mode of back through second grade water heat exchanger and crude benzol distillation unit condensate water heat transfer has realized thermal step recycle.
Drawings
Figure 1 is the schematic diagram of the low grade waste heat recovery system of the coking production system of the present invention.
In the figure: 1. supplementing secondary demineralized water 2, a demineralized water tank 3, a steam extraction condensing steam turbine 4, a condenser 5, circulating cooling water 6, a condensate pump 7, a deoxygenation water feed pump 8, a water feed preheater 9, a primary water-water heat exchanger 10, a secondary water-water heat exchanger 11, a deoxygenator 12, a boiler water feed pump 13, an economizer 14, a steam pocket 15, a membrane water wall and an evaporator 16, a primary superheater 17, a water spray desuperheater 18, a secondary superheater 19, a crude benzene distillation unit 20, a plant low-pressure steam pipe network 21, a demineralized water station 22, a continuous blowdown expander 23, a blowdown pump 24, a dry quenching device water seal tank 25, a generator 26, an inert circulating gas inlet 27, an inert circulating gas outlet 27, a steam extraction condensing steam turbine 4, a condenser 5, circulating cooling water 6, a condensate pump 7, a steam pocket 15, a primary superheater 17, a water spray desuperheater 18, a secondary superheater 19, a crude benzene distillation unit 20, a plant low-pressure steam pipe network 21, a demineralized water station 22, a continuous blowdown expander 23, a dry quenching device water seal tank 25, a generator 26, an inert circulating gas outlet 27, a dry quenching device, a steam generator
Detailed Description
The working principle of the low-grade waste heat recovery system of the coking production system is as follows:
1) the condensed water of the crude benzene distillation unit indirectly exchanges heat with the deoxygenated return water, the deoxygenated return water temperature is improved, the heating steam amount of a deoxygenator is saved, and the waste heat of the condensed water of the crude benzene distillation unit is recovered;
2) conveying the flash steam of the crude benzene distillation unit to a plant low-pressure steam pipe network (without being limited to the mode), and recovering the waste heat of the flash steam of the crude benzene distillation unit;
3) the sewage of the continuous sewage disposal expander indirectly exchanges heat with the deoxygenation backwater, so that the deoxygenation backwater temperature is increased, the heating steam quantity of the deoxygenator is saved, and the waste heat of the sewage is recovered;
4) and secondary steam of the continuous blowdown expander is sent to the deaerator to directly exchange heat with the deaerating return water, so that the deaerating return water temperature is increased, the heating steam quantity of the deaerator is saved, and the waste heat of the secondary steam is recovered.
The following description of the embodiments of the present invention will be made with reference to the accompanying drawings:
as shown in fig. 1, the utility model relates to a low-grade waste heat recovery system of coking production system, the coking production system includes dry quenching boiler, steam extraction condensing steam turbine 3, condenser 4, condensate pump 6, generator 25, crude benzene distillation unit 19, oxygen-eliminating device 11, deoxidization water-feeding pump 7, demineralized water tank 2, demineralized water station 21, boiler water-feeding pump 12, continuous blowdown expander 22, dredge pump 23 and dry quenching device water seal tank 24; an inert circulating gas inlet 26 is formed in the top of the dry quenching boiler, an inert circulating gas outlet 27 is formed in the bottom of the dry quenching boiler, and a feed water preheater 8 is arranged at the position of the inert circulating gas outlet 27; an economizer 13, a membrane water wall and evaporator 15, a primary superheater 16 and a secondary superheater 18 are sequentially arranged in the coke dry quenching boiler from bottom to top, the primary superheater 16 is connected with the secondary superheater 18 through a water-spraying desuperheater 17, and the economizer 13, the membrane water wall and evaporator 15 and the primary superheater 16 are respectively connected with a steam drum 14; the steam drum 14 is provided with a continuous blowdown expander 22; the low-grade waste heat recovery system comprises a primary water-water heat exchanger 9 and a secondary water-water heat exchanger 10; the desalting water tank 2 is provided with a secondary desalting water inlet, a condensed water inlet and a boiler water supply outlet; the boiler water supply outlet is sequentially connected with a deoxidizing water supply pump 7, a water supply preheater 8, a primary water-water heat exchanger 9, a secondary water-water heat exchanger 10, a deaerator 11, a boiler water supply pump 12, an economizer 13 and a steam drum 14 through a boiler water supply pipeline; the steam drum 14 is respectively connected with a boiler water supply inlet of the membrane water-cooling wall and a boiler water supply inlet of the evaporator through a downcomer, and a steam-water mixture outlet of the membrane water-cooling wall and a steam-water mixture outlet of the evaporator are respectively connected with a steam-water mixture inlet of a steam-water separation device in the steam drum 14; a saturated steam outlet of the steam-water separation device is connected with a steam inlet of the primary superheater 16 through a collecting pipe, an superheated steam outlet of the primary superheater 16 is connected with a steam inlet of the water spray desuperheater 17, a steam outlet of the water spray desuperheater 17 is connected with a steam inlet of the secondary superheater 18, and an superheated steam outlet of the secondary superheater 18 is connected with a superheated steam inlet of the steam extraction condensing steam turbine 3; a superheated steam outlet of the steam extraction condensing steam turbine 3 is connected with a steam inlet of the crude benzene distillation unit 19; the exhaust steam outlet of the steam extraction and condensation type steam turbine 3 is sequentially connected with the condenser 4, the condensate pump 6 and the condensate inlet of the desalting water tank 2 through a condensate water pipeline; a condensed water outlet of the crude benzene distillation unit 19 is sequentially connected with the secondary water-water heat exchanger 10 and the desalted water station 21 through a condensed water pipeline; the continuous expansion blowdown device 22 is sequentially connected with a primary water-water heat exchanger 9, a blowdown pump 23 and a dry quenching device water seal tank 24 through a blowdown pipeline.
The feed water preheater 8 is a radial heat exchange tube feed water preheater.
The dredge pump 23 is a long-axis submerged dredge pump.
The first-stage water-water heat exchanger 9 and the second-stage water-water heat exchanger 10 are both shell-and-tube heat exchangers.
The technical process of the low-grade waste heat recovery system of the coking production system is as follows:
1) the supplementary secondary desalted water 1 which is supplied from the outside and has the temperature of 25-30 ℃ directly enters the desalted water tank 2; after the waste steam which does work by the steam extraction condensing steam turbine 3 exchanges heat with circulating cooling water 5 through a condenser 4, the temperature of returned condensed water is 40-45 ℃, the condensed water enters a desalting water tank 2 through a condensed water pump 6, and the waste steam is mixed with supplementary secondary desalting water in the desalting water tank 2 to be used as boiler feed water;
2) boiler feed water is pressurized and sent to a dry quenching boiler by a deoxygenation feed water pump 7, is heated to 60-70 ℃ by a feed water preheater 8, is sent to a primary water-water heat exchanger 9, is heated to 61-71 ℃ after heat exchange, is sent to a secondary water-water heat exchanger 10, is heated to 70-80 ℃ after heat exchange, and finally enters a deoxygenator 11 to be heated to ensure that the water temperature is raised to over 104 ℃, and is pressurized and sent to an economizer 13 by a boiler feed water pump 12;
3) boiler feed water is subjected to heat exchange through an economizer 13 to ensure that the temperature of the water is increased to more than 260 ℃, then the water enters a steam drum 14, the saturation temperature of furnace water in the steam drum 14 is more than 315 ℃, the furnace water respectively enters a membrane water-cooled wall and an evaporator 15 of a dry quenching boiler through a downcomer, and a steam-water mixture is formed after heat absorption and vaporization and enters the steam drum 14 under the action of hot pressing;
4) the steam-water mixture is separated by a steam-water separation device in a steam drum 14 to generate saturated steam, the saturated steam enters a primary superheater 15 through a collecting pipe to exchange heat with high-temperature inert circulating gas to generate superheated steam with the temperature higher than a set temperature, and the temperature of the superheated steam is adjusted to the set temperature through a water-spraying desuperheater 17; the superheated steam after temperature adjustment enters a secondary superheater 18, and exchanges heat with high-temperature inert circulating gas to raise the temperature, and finally the temperature of the superheated steam reaches over 540 ℃;
5) the superheated steam which is subjected to heat exchange and temperature rise by the secondary superheater 18 completely enters the steam extraction condensing steam turbine 3, and is used for generating electricity by the generator 25, and one path of superheated steam with the temperature of more than 450 ℃ is extracted and supplied to the crude benzene distillation unit 19;
6) superheated steam flashed to above 165 ℃ by the crude benzene distillation unit 19 is sent to a plant low-pressure steam pipe network 20, condensed water generated by the crude benzene distillation unit 19 is sent to a desalted water station 21 after heat exchange by a secondary water-water heat exchanger 10, and is recycled after treatment;
7) steam for heating the deaerator 11 is connected with a plant area low-pressure steam pipe network 20; the sewage discharged by the continuous blowdown expander 22 is subjected to heat exchange by the primary water-water heat exchanger 9 and then is sent to a water seal tank 24 of a dry quenching device by a blowdown pump 23.
The condenser 4 cools the exhaust steam of the steam extraction condensing steam turbine 3 by adopting an air cooling mode or a water cooling mode.
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 (4)
1. A low-grade waste heat recovery system of a coking production system comprises a dry quenching boiler, a steam extraction and condensing steam turbine, a condenser, a condensing water pump, a generator, a crude benzene distillation unit, a deaerator, a deaerating water feed pump, a desalting water tank, a desalting water station, a boiler water feed pump, a continuous blowdown expander, a blowdown pump and a dry quenching device water seal tank; the top of the dry quenching boiler is provided with an inert circulating gas inlet, the bottom of the dry quenching boiler is provided with an inert circulating gas outlet, and the inert circulating gas outlet is provided with a feed water preheater; the dry coke quenching boiler is internally provided with an economizer, a membrane water wall, an evaporator, a primary superheater and a secondary superheater from bottom to top in sequence, the primary superheater and the secondary superheater are connected through a water-spraying type desuperheater, and the economizer, the membrane water wall, the evaporator and the primary superheater are respectively connected with a steam drum; the steam pocket is provided with a continuous blowdown expander; the low-grade waste heat recovery system is characterized by comprising a primary water-water heat exchanger and a secondary water-water heat exchanger; the desalting water tank is provided with a secondary desalting water inlet, a condensed water inlet and a boiler water supply outlet; the boiler water supply outlet is sequentially connected with a deoxidizing water supply pump, a water supply preheater, a primary water-water heat exchanger, a secondary water-water heat exchanger, a deaerator, a boiler water supply pump, an economizer and a steam drum through a boiler water supply pipeline; the steam pocket is respectively connected with a boiler water supply inlet of the membrane water-cooling wall and a boiler water supply inlet of the evaporator through a downcomer, and a steam-water mixture outlet of the membrane water-cooling wall and a steam-water mixture outlet of the evaporator are respectively connected with a steam-water mixture inlet of a steam-water separation device in the steam pocket; a saturated steam outlet of the steam-water separation device is connected with a steam inlet of a primary superheater through a collecting pipe, an overheated steam outlet of the primary superheater is connected with a steam inlet of a water spray desuperheater, a steam outlet of the water spray desuperheater is connected with a steam inlet of a secondary superheater, and an overheated steam outlet of the secondary superheater is connected with an overheated steam inlet of a steam extraction condensing steam turbine; a superheated steam outlet of the steam extraction condensing steam turbine is connected with a steam inlet of the crude benzene distillation unit; the waste steam outlet of the steam extraction and condensation type steam turbine is sequentially connected with a condenser, a condensate pump and a condensate inlet of a desalting water tank through a condensate water pipeline; a condensed water outlet of the crude benzene distillation unit is sequentially connected with a secondary water-water heat exchanger and a desalted water station through a condensed water pipeline; the continuous blowdown expander is sequentially connected with the primary water-water heat exchanger, the blowdown pump and the water seal tank of the dry quenching device through a blowdown pipeline.
2. The low-grade waste heat recovery system of a coking production system according to claim 1, characterized in that the feed water preheater is a radial heat exchange tube feed water preheater.
3. A low grade waste heat recovery system of a coking production system according to claim 1, characterised in that the dredge pump is a long shaft submerged dredge pump.
4. The low-grade waste heat recovery system of the coking production system according to claim 1, characterized in that the primary water-water heat exchanger and the secondary water-water heat exchanger are both shell-and-tube heat exchangers.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112610941A (en) * | 2020-12-30 | 2021-04-06 | 中冶焦耐(大连)工程技术有限公司 | Low-grade waste heat recovery system and process of coking production system |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112610941A (en) * | 2020-12-30 | 2021-04-06 | 中冶焦耐(大连)工程技术有限公司 | Low-grade waste heat recovery system and process of coking production system |
| CN112610941B (en) * | 2020-12-30 | 2024-10-01 | 中冶焦耐(大连)工程技术有限公司 | Low-grade waste heat recovery system and process of coking production system |
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