CN116658908A - Waste incineration power plant electric power consumption system based on incineration fly ash regenerated salt heat storage - Google Patents
Waste incineration power plant electric power consumption system based on incineration fly ash regenerated salt heat storage Download PDFInfo
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- 150000003839 salts Chemical class 0.000 title claims abstract description 339
- 238000005338 heat storage Methods 0.000 title claims abstract description 37
- 238000004056 waste incineration Methods 0.000 title claims abstract description 35
- 239000010881 fly ash Substances 0.000 title claims abstract description 29
- 239000003546 flue gas Substances 0.000 claims abstract description 81
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 80
- 239000003381 stabilizer Substances 0.000 claims abstract description 60
- 238000010248 power generation Methods 0.000 claims abstract description 24
- 238000000605 extraction Methods 0.000 claims abstract description 7
- 239000000779 smoke Substances 0.000 claims description 40
- 238000000034 method Methods 0.000 claims description 19
- 230000008018 melting Effects 0.000 claims description 13
- 238000002844 melting Methods 0.000 claims description 13
- 230000001105 regulatory effect Effects 0.000 claims description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 11
- HGUFODBRKLSHSI-UHFFFAOYSA-N 2,3,7,8-tetrachloro-dibenzo-p-dioxin Chemical compound O1C2=CC(Cl)=C(Cl)C=C2OC2=C1C=C(Cl)C(Cl)=C2 HGUFODBRKLSHSI-UHFFFAOYSA-N 0.000 claims description 10
- 150000003841 chloride salts Chemical class 0.000 claims description 9
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims description 8
- 239000007789 gas Substances 0.000 claims description 8
- 238000005406 washing Methods 0.000 claims description 7
- 238000005485 electric heating Methods 0.000 claims description 6
- 230000005496 eutectics Effects 0.000 claims description 6
- 230000002035 prolonged effect Effects 0.000 claims description 5
- 238000002425 crystallisation Methods 0.000 claims description 4
- 230000008025 crystallization Effects 0.000 claims description 4
- 238000000746 purification Methods 0.000 claims description 4
- 239000011780 sodium chloride Substances 0.000 claims description 4
- 238000000354 decomposition reaction Methods 0.000 claims description 3
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- 239000000203 mixture Substances 0.000 claims description 3
- 230000000087 stabilizing effect Effects 0.000 claims description 3
- 239000002918 waste heat Substances 0.000 claims description 3
- 238000001816 cooling Methods 0.000 claims description 2
- 238000010828 elution Methods 0.000 claims description 2
- 238000001704 evaporation Methods 0.000 claims description 2
- ZZUFCTLCJUWOSV-UHFFFAOYSA-N furosemide Chemical compound C1=C(Cl)C(S(=O)(=O)N)=CC(C(O)=O)=C1NCC1=CC=CO1 ZZUFCTLCJUWOSV-UHFFFAOYSA-N 0.000 claims description 2
- 238000002386 leaching Methods 0.000 claims description 2
- 238000005086 pumping Methods 0.000 claims description 2
- 230000008020 evaporation Effects 0.000 claims 1
- 239000002699 waste material Substances 0.000 abstract description 10
- 238000005516 engineering process Methods 0.000 abstract description 8
- 238000011049 filling Methods 0.000 abstract description 3
- 239000000460 chlorine Substances 0.000 abstract description 2
- 229910052801 chlorine Inorganic materials 0.000 abstract description 2
- 238000004146 energy storage Methods 0.000 description 13
- 230000008569 process Effects 0.000 description 10
- 239000011232 storage material Substances 0.000 description 8
- 230000033228 biological regulation Effects 0.000 description 6
- 238000006243 chemical reaction Methods 0.000 description 5
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- 230000004048 modification Effects 0.000 description 5
- 229910002651 NO3 Inorganic materials 0.000 description 4
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 4
- 230000008929 regeneration Effects 0.000 description 4
- 238000011069 regeneration method Methods 0.000 description 4
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 3
- 238000007792 addition Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000001640 fractional crystallisation Methods 0.000 description 3
- 229910001385 heavy metal Inorganic materials 0.000 description 3
- 230000006872 improvement Effects 0.000 description 3
- 238000002360 preparation method Methods 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 238000000197 pyrolysis Methods 0.000 description 3
- 238000004064 recycling Methods 0.000 description 3
- 238000007789 sealing Methods 0.000 description 3
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- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 2
- 231100000770 Toxic Equivalency Factor Toxicity 0.000 description 2
- 229910052791 calcium Inorganic materials 0.000 description 2
- 239000011575 calcium Substances 0.000 description 2
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- 239000003344 environmental pollutant Substances 0.000 description 2
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- 231100000719 pollutant Toxicity 0.000 description 2
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- 238000012546 transfer Methods 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 230000003416 augmentation Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 159000000007 calcium salts Chemical class 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 150000001804 chlorine Chemical class 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
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- 230000029087 digestion Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000009977 dual effect Effects 0.000 description 1
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- 239000007788 liquid Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
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- 239000012466 permeate Substances 0.000 description 1
- 239000002957 persistent organic pollutant Substances 0.000 description 1
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- 238000011084 recovery Methods 0.000 description 1
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- 238000012360 testing method Methods 0.000 description 1
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Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
- F23G5/44—Details; Accessories
- F23G5/46—Recuperation of heat
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/06—Arrangements of devices for treating smoke or fumes of coolers
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F24—HEATING; RANGES; VENTILATING
- F24H—FLUID HEATERS, e.g. WATER OR AIR HEATERS, HAVING HEAT-GENERATING MEANS, e.g. HEAT PUMPS, IN GENERAL
- F24H1/00—Water heaters, e.g. boilers, continuous-flow heaters or water-storage heaters
- F24H1/18—Water-storage heaters
- F24H1/20—Water-storage heaters with immersed heating elements, e.g. electric elements or furnace tubes
- F24H1/201—Water-storage heaters with immersed heating elements, e.g. electric elements or furnace tubes using electric energy supply
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D20/00—Heat storage plants or apparatus in general; Regenerative heat-exchange apparatus not covered by groups F28D17/00 or F28D19/00
- F28D20/0034—Heat storage plants or apparatus in general; Regenerative heat-exchange apparatus not covered by groups F28D17/00 or F28D19/00 using liquid heat storage material
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F27/00—Control arrangements or safety devices specially adapted for heat-exchange or heat-transfer apparatus
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D20/00—Heat storage plants or apparatus in general; Regenerative heat-exchange apparatus not covered by groups F28D17/00 or F28D19/00
- F28D20/0034—Heat storage plants or apparatus in general; Regenerative heat-exchange apparatus not covered by groups F28D17/00 or F28D19/00 using liquid heat storage material
- F28D2020/0047—Heat storage plants or apparatus in general; Regenerative heat-exchange apparatus not covered by groups F28D17/00 or F28D19/00 using liquid heat storage material using molten salts or liquid metals
Landscapes
- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Engine Equipment That Uses Special Cycles (AREA)
Abstract
The invention relates to a garbage incineration and fused salt heat storage technology, and aims to provide a garbage incineration power plant power consumption system based on regenerated salt heat storage of incineration fly ash. The system comprises a flue gas temperature stabilizer and a flue gas-molten salt heat exchanger which are arranged in a flue, wherein both the flue gas temperature stabilizer and the molten salt-steam reheater take molten salt as an internal heat exchange medium, and an external heat exchange medium of the flue gas temperature stabilizer and the flue gas-molten salt heat exchanger is steam from an extraction opening of a steam turbine; the top of the high-temperature molten salt tank is sequentially connected with a molten salt pump, a molten salt-steam reheater and a molten salt inlet at the top of the low-temperature molten salt tank through pipelines; the outlet at the bottom of the low-temperature molten salt tank is divided into two paths, one path is sequentially connected with the molten salt pump, the flue gas-molten salt heat exchanger, the flue gas temperature stabilizer and the high-temperature molten salt tank, and the other path is sequentially connected with the molten salt pump, the electric heater and the high-temperature molten salt tank. According to the invention, the stable output power of the waste incineration power plant and peak clipping and valley filling are realized through the fused salt heat storage, and the power generation allowance of the power plant is consumed; realizes the efficient reuse of high-chlorine waste salt in the waste incineration fly ash, and has the advantages of cleanness, no pollution and low cost.
Description
Technical Field
The invention relates to the technical field of garbage incineration and fused salt heat storage, in particular to a garbage incineration power plant power consumption system based on regenerated salt heat storage of incineration fly ash.
Background
In the dual carbon context, renewable new energy has become the main body of new electric power augmentation machines. And as the fluctuation of the new energy power generation amount is large, the periodic load fluctuation of the power grid is increased. Under the background, the capacity of "wind abandon" and "light abandon" becomes a constraint factor for further development of new energy, so that each power plant also takes on the tasks of energy storage peak regulation and electricity abandon and digestion correspondingly.
Because the garbage incineration has the advantages of good capacity reduction, high harmless degree, energy recovery and the like, the garbage incineration is commonly used for power generation and also belongs to a new energy power generation technology. However, the incinerator has the problems of unstable flue gas temperature and difficult regulation and control due to large characteristic changes of the garbage combustion heat value, the water content, the garbage amount and the like, and waste of the super-generated energy and increase of the heat loss of the discharged smoke are easy to cause. Therefore, the waste incineration power plant lacks energy storage peak shaving capability and also places a larger burden on the power grid. In order to avoid electric power waste, the energy storage peak shaving capacity needs to be improved, the load of a power grid is reduced, and the capacity of new energy power generation allowance consumption is contributed.
In the main energy storage technology, the pumped storage and heat storage technology has high energy conversion rate of electric energy, reliable technology and low cost, and is suitable for energy storage peak shaving of a power plant. The pumped storage has long service life, large capacity and long energy storage period. However, the garbage incineration power plants are generally arranged in the surrounding areas of cities and towns, so that pumped storage is limited by natural conditions, cannot be popularized and applied in plain areas, and cannot meet the energy storage requirements of the garbage incineration power plants with relatively small scale.
The heat storage technology represented by molten salt has small occupied area, high energy storage density and easy coupling with a power generation system. However, the conventional molten salt material belongs to a nitrate system, is easy to decompose at high temperature, and has lower heat storage grade and higher cost. Therefore, the mainstream molten salt heat storage system is generally used for low-temperature heat storage occasions in the photo-thermal power station, is not suitable for the garbage incinerator, and has no improvement effect on the operating conditions of the incinerator.
In summary, various defects in the prior art lead to incapability of adapting to the current clean energy storage peak regulation requirement of the waste incineration power plant, and incapability of realizing incineration performance optimization and regeneration salt utilization. Therefore, it is necessary to develop a new energy storage system, which can fully utilize the characteristics of the regenerated salt of the fly ash to realize flexible peak regulation and power consumption based on the characteristics of the waste incineration power plant.
Disclosure of Invention
The invention aims to solve the technical problem of overcoming the defects of the prior art and providing a waste incineration power plant electric power consumption system based on regenerated salt heat storage of incineration fly ash.
In order to solve the technical problems, the invention adopts the following solutions:
the electric power consumption system of the waste incineration power plant based on the regenerated salt heat storage of the incineration fly ash comprises a high-temperature salt melting tank and a low-temperature salt melting tank which are arranged in the waste incineration power plant, and a smoke temperature stabilizer, a smoke-fused salt heat exchanger, a fused salt-steam reheater and an electric heater which are used as heat exchange equipment; wherein,,
the flue gas temperature stabilizer and the flue gas-molten salt heat exchanger are sequentially arranged in a flue behind the incinerator along the flue gas flow direction, and both take flue gas as an external heat exchange medium and molten salt as an internal heat exchange medium; the internal heat exchange medium of the fused salt-steam reheater is fused salt, the external heat exchange medium is steam from an extraction opening of a steam turbine, and the steam turbine is connected with a generator set of the waste incineration power plant; by a means ofThe fused salt is regenerated salt obtained by water washing, salt leaching and evaporative crystallization of waste incineration fly ash, and has a melting point of less than or equal to 550 ℃ and 1.01X10 5 5h mass loss at Pa and 850 ℃<5, thereby meeting the heat storage operation requirement within the temperature range of 600-850 ℃;
the molten salt outlet arranged at the top of the high-temperature molten salt tank is sequentially connected with a molten salt pump, a molten salt-steam reheater and a molten salt inlet at the top of the low-temperature molten salt tank through pipelines; two molten salt outlets are arranged at the bottom of the low-temperature molten salt tank, one outlet is sequentially connected with a molten salt pump, a flue gas-molten salt heat exchanger, a flue gas temperature stabilizer and a molten salt inlet at the bottom of the high-temperature molten salt tank through pipelines, and the other outlet is sequentially connected with the molten salt pump, an electric heater and the molten salt inlet at the bottom of the high-temperature molten salt tank through pipelines.
As a preferable scheme of the invention, the main bodies of the high-temperature molten salt tank and the low-temperature molten salt tank are cylinder bodies with sealing structures, and an electric heating module is arranged outside the cylinder bodies in a surrounding mode.
As a preferable scheme of the invention, all electric equipment in the system is connected to a power supply system of the garbage incineration power plant through a cable, so that self-power generation supply is realized.
As a preferable mode of the present invention, the electric heater is further connected to an external power source through a cable, the external power source being a wind power generation device, a photovoltaic power generation device, a hydro power generation device, or a public power grid.
As a preferred scheme of the invention, in the flue gas-molten salt heat exchanger, flue gas and molten salt are arranged in countercurrent; in the molten salt-steam reheater, the molten salt is arranged in countercurrent with steam; in the smoke temperature stabilizer, the smoke and molten salt are arranged in parallel flow; a bypass pipeline is arranged between the molten salt inlet and outlet of the smoke temperature stabilizer.
The invention further provides a method for realizing heat storage and power consumption of regenerated salt of a waste incineration power plant by using the system, which comprises the following steps:
(1) The flue gas at the outlet of the incinerator hearth of the garbage incineration power plant sequentially flows through a flue gas temperature stabilizer and a flue gas-molten salt heat exchanger, and enters a tail gas purification system after exchanging heat with molten salt in the flue gas temperature stabilizer and the flue gas-molten salt heat exchanger;
(2) The steam from the steam extraction port of the steam turbine enters a fused salt-steam reheater to exchange heat with fused salt extracted from a high-temperature fused salt tank, and the warmed steam is sent back to the steam turbine to release heat and do work for power generation; the molten salt after cooling is sent into a low-temperature molten salt tank;
(3) Pumping molten salt from the low-temperature molten salt tank, and respectively sending the molten salt to an electric heater and a flue gas-molten salt heat exchanger; the molten salt is heated in the electric heater for consuming the power allowance of the power plant or external power supply; the molten salt exchanges heat with the flue gas in a flue gas-molten salt heat exchanger in a countercurrent way, and is used for absorbing the waste heat of the flue gas; then continuously sending the mixture into a smoke temperature stabilizer to exchange heat with smoke in concurrent flow for stabilizing the temperature of the smoke; the molten salt which is heated further after absorbing heat is sent back to the high-temperature molten salt tank for reducing the non-uniformity of temperature distribution in the tank;
(4) In the flue gas temperature stabilizer, part of molten salt flows back to the inflow port from the outlet through the bypass pipe, and is used for adjusting the flow rate of the molten salt to stabilize the temperature of flue gas, so that the residence time of the flue gas in a temperature region above 850 ℃ is prolonged to at least 5 seconds, and the decomposition of organic matters including dioxin is promoted.
As a preferable scheme of the invention, the molten salt temperatures in the high-temperature molten salt tank and the low-temperature molten salt tank are controlled to be 850+/-20 ℃ and 600+/-15 ℃ respectively; the temperature of molten salt at the inlet of the smoke temperature stabilizer is 800+/-10 ℃, and the temperature of molten salt at the outlet of the smoke temperature stabilizer is 850+/-10 ℃; the molten salt temperatures at the outlets of the flue gas-molten salt heat exchanger, the molten salt-steam reheater and the electric heater are respectively consistent with the molten salt temperatures at the corresponding reaching positions.
As a preferable scheme of the invention, the external heat exchange medium of the smoke temperature stabilizer is smoke at the outlet of the hearth of the incinerator, the temperature of the inlet side of the smoke temperature stabilizer is 950+/-50 ℃, and the temperature of the outlet side of the smoke temperature stabilizer is 850+/-10 ℃; the external heat exchange medium of the flue gas-molten salt heat exchanger is flue gas from the outlet of the flue gas temperature stabilizer, the temperature of the inlet side of the flue gas-molten salt heat exchanger is 850+/-10 ℃, and the temperature of the outlet side of the flue gas-molten salt heat exchanger is 650+/-15 ℃; the temperature of the pipe wall of the electric heater is 950+/-50 ℃; on the steam side of the molten salt-steam reheater, the steam parameters at the inlet are 0.6MPa and 248 ℃, and the steam parameters at the outlet are 3.82MPa and 435 ℃.
As a preferable scheme of the invention, valves are utilized to control the flow of molten salt entering the flue gas-molten salt heat exchanger, the molten salt-steam reheater, the electric heater and the bypass pipeline of the flue gas temperature stabilizer; the flow of molten salt of the flue gas-molten salt heat exchanger is regulated according to the temperature of the molten salt at the outlet side; the molten salt flow of the molten salt-steam reheater is adjusted according to the steam temperature at the outlet side; the molten salt flow of the electric heater is regulated according to the molten salt temperature at the outlet side; and the molten salt flow of the bypass pipeline of the smoke temperature stabilizer is regulated according to the smoke temperature at the outlet side.
As a preferable scheme of the invention, the fused salt is regenerated salt generated by evaporating and crystallizing after salt elution of fly ash water from garbage incineration, and the components comprise NaCl, KCl and CaCl 2 Is a ternary eutectic chloride salt of (2); the melting point of the ternary eutectic chloride salt is less than or equal to 550 ℃ and is 1.01X10 5 5h mass loss at Pa and 850 ℃<5％。
Description of the inventive principles:
the fused salt heat storage is a peak shaving mode with high efficiency, energy saving and high reliability, can effectively stabilize the output power of a power plant, cut peaks and fill valleys of periodically fluctuating loads and reduce light and wind abandoning. The waste incineration power plant lacks load adjusting capability and has serious waste of salt in fly ash due to large fluctuation of output power.
The content of chloride salt in the waste incineration fly ash accounts for 25-50%, so that the waste incineration fly ash is easy to permeate into soil and underground water along with precipitation, serious adverse effects are caused on a fly ash disposal process, and proper disposal is a key ring of harmless disposal and recycling of the fly ash. In general, fly ash chloride salt is separated by water washing, and waste water from water washing is evaporated and crystallized to produce waste salt for landfill or fractional crystallization to extract pure salt. The landfill method faces the elimination, the existing fractional crystallization process route has the problems of high energy consumption, great waste of calcium salt, great production of heavy metal-containing sediment and low product acceptance, and a fly ash regenerated salt integrated utilization method is needed to realize efficient regeneration. The fly ash regenerated salt belongs to NaCl-KCl-CaCl 2 Compared with nitrate, the multi-chlorine salt system has higher upper limit of use temperature, so that the high-grade heat energy of the waste incinerator flue gas can be stored, and higher heat-electricity conversion rate can be achieved.
Therefore, the invention couples the fused salt heat storage with the waste incineration power plant, adopts the novel regenerated salt extracted from the waste incineration fly ash as a low-cost clean heat storage medium, can consume the power generation allowance of the power plant, and realizes the stable output power, peak clipping and valley filling, the consumption and the electric abandonment, the clean energy storage, the improvement of the heat efficiency and the stabilization of the working condition of the heat exchanger.
The main technical principle of the invention is as follows:
energy storage peak regulation and combustion improvement
(1) During a load peak, starting the fused salt-steam reheater to generate high-pressure steam for power generation; at low load, the molten salt-steam reheater stops operating. And controlling the molten salt flow entering the flue gas-molten salt heat exchanger, the molten salt-steam reheater, the electric heater and the flue gas temperature stabilizer bypass pipeline by using a valve. Wherein: the flow of molten salt of the flue gas-molten salt heat exchanger is regulated according to the temperature of the molten salt at the outlet side, so that the heat exchange amount is ensured; the molten salt flow of the molten salt-steam reheater is regulated according to the steam temperature at the outlet side, so that the steam inlet temperature of the steam turbine is ensured; and regulating the flow of the molten salt of the electric heater according to the temperature of the molten salt at the outlet side, and maintaining the temperature of the molten salt at the outlet. And the flow of molten salt in the bypass pipeline of the smoke temperature stabilizer is regulated according to the smoke temperature at the outlet side, so that the smoke temperature at the outlet is stabilized.
(2) The first low-temperature molten salt pump conveys low-temperature molten salt in the low-temperature molten salt tank to the flue gas-molten salt heat exchanger, and the flue gas is conveyed to the flue gas temperature stabilizer for further heat exchange after the residual temperature of the flue gas is absorbed; the fused salt after absorbing the heat of the high-temperature flue gas is stored in a high-temperature fused salt tank, and the heat storage grade is high. The second low-temperature molten salt pump conveys molten salt in the low-temperature molten salt tank to the electric heater, and the heated molten salt is stored in the high-temperature molten salt tank, so that the power generation allowance of a power plant or an external power supply system can be consumed. The high-temperature molten salt pump conveys molten salt in the high-temperature molten salt tank to the flue gas-steam reheater to release heat, and the high-temperature molten salt pump is used for producing high-temperature and high-pressure steam which can meet the steam inlet requirement of the steam turbine.
(3) The essence of the smoke temperature stabilizer is a high-temperature heat exchanger which is used for increasing the turbulence degree of a high-temperature flue and prolonging the residence time of the high temperature, and can play a role in covering the surface of the high-temperature flue and protecting the wall surface of the flue. By using the smoke temperature stabilizer and the smoke-molten salt heat exchanger in combination, the temperature fluctuation of smoke in the flue is small, the working state of the heating surface of the flue is stable, and the fluctuation of the smoke discharging temperature is small. Therefore, the invention can solve the problems of high heat loss, regeneration of dioxin and thermal desorption of the fly ash dioxin caused by the excessive high exhaust gas temperature and aggravated low-temperature corrosion caused by the low exhaust gas temperature. The residence time of the flue gas at the temperature of above 850 ℃ can be prolonged, and the pyrolysis of dioxin is promoted; and a lower design value of the exhaust gas temperature can be realized, and inherent exhaust gas heat loss is reduced.
(II) novel regenerated salt clean heat storage material
(1) The conventional fused salt heat storage material generally uses polybasic nitrate, and the operating temperature of the conventional fused salt heat storage material is usually 250-600 ℃, so that the conventional fused salt heat storage material has the characteristic of pyrolysis and is not suitable for high-temperature flue gas heat storage. The polybasic chlorine salt adopted by the invention has relatively higher melting point and stronger thermal stability, and can be operated at 600-850 ℃. Therefore, the heat storage grade is higher, the cost is lower, the heat-electricity conversion rate is improved, and the heat storage material is a novel fused salt heat storage material.
(2) The waste incineration fly ash contains a large amount of NaCl, KCl and CaCl 2 In the treatment process, the salt is usually extracted by a water washing mode, and the water washing waste liquid is evaporated and crystallized to obtain the multi-element mixed chloride salt, so that the cost is far lower than that of a finished product of single salt or multi-element nitrate. Compared with the traditional process, the regeneration salt heat storage utilization provides an application scene of integrating the fly ash and the chloride, does not need to remove all calcium, has high recycling rate, avoids high-energy-consumption fractional crystallization, and provides a new efficient energy-saving scheme for the fly ash and chloride recycling process.
(3) Dioxin and other organic pollutants in the waste salt are thoroughly degraded through high-temperature heat treatment, and the escape risk of heavy metals and other pollutants is avoided in a closed operation environment. Through the integrated application, a large amount of calcium-based sediment containing heavy metals is prevented from being generated in the treatment process of the regenerated salt.
Compared with the prior art, the invention has the following beneficial effects:
(1) According to the invention, through fused salt heat storage, the output power stability, peak clipping and valley filling of the waste incineration power plant can be realized, and the power generation allowance of the power plant can be consumed.
(2) The fused salt adopted by the invention is used as a high-temperature heat exchange medium, is safe and stable, and has high energy storage grade and high heat-electricity conversion rate.
(3) The invention can directly recycle and use the fused salt in the waste incineration power plant, realizes the efficient reuse of the high-chlorine waste salt in the waste incineration fly ash, is clean and pollution-free, and has low cost of heat storage materials.
(4) The invention can stabilize the temperature of the flue gas, improve the working condition of a heat exchange surface, reduce the emission of dioxin and other pollutants and consume the regenerated salt of the fly ash.
Drawings
FIG. 1 is a process flow diagram of the present invention.
Fig. 2 is a schematic diagram of a system structure according to the present invention.
The reference numerals in the drawings are: 1-high temperature molten salt tank, 2-low temperature molten salt tank, 3-molten salt-steam reheater, 4-flue gas-molten salt heat exchanger, 5-flue gas temperature stabilizer, 6-electric heater, 7-high temperature molten salt pump, 8-first low temperature molten salt pump, 9-second low temperature molten salt pump, 10-high temperature molten salt valve, 11-first low temperature molten salt valve, 12-second low temperature molten salt valve, 13-bypass valve.
Detailed Description
The main heat exchange medium used in the invention is molten salt, and the regenerated salt obtained by water washing salt and evaporative crystallization of the waste incineration fly ash contains NaCl, KCl and CaCl 2 Is a ternary eutectic chloride salt of (a). The preparation process of the molten salt can adopt the prior public technology, such as the molten salt processing technology recorded in the Chinese patent application of ternary chloride molten salt with high-temperature heat stability and a preparation method thereof (bulletin number: CN 113372886A). The invention only provides the product performance requirements for the molten salt: melting point is less than or equal to 550 ℃, and is 1.01X10% 5 5h mass loss at Pa and 850 ℃<5, thereby meeting the heat storage operation requirement within the temperature range of 600-850 ℃. As for the specific component proportion relation and production process parameters of the molten salt, the invention does not need to be specially required.
In the invention, the main bodies of the high-temperature molten salt tank and the low-temperature molten salt tank are cylinder bodies with sealing structures, and an electric heating module is arranged on the outer periphery of each cylinder body; the high temperature and the low temperature only represent the difference of the temperature of the molten salt in the molten salt tank. The temperature can be realized by adjusting the heat exchange quantity of the heat exchange equipment connected with the tank body and the flue gas and adjusting the power of the external electric heating module, and no special distinguishing requirement is required for the tank body. The same holds true for the definition of high and low temperatures of the molten salt pump hereinafter. In addition, the flue gas temperature stabilizer, the flue gas-molten salt heat exchanger, the molten salt-steam reheater and the electric heater are all heat exchange equipment, and related equipment is processed in a conventional mode.
The invention is further illustrated by the following examples in conjunction with the accompanying drawings, without limiting the invention.
As shown in fig. 1 and 2, the electric power consumption system of the waste incineration power plant comprises a high-temperature molten salt tank 1 and a low-temperature molten salt tank 2 which are arranged in the waste incineration power plant, and a molten salt-steam reheater 3, a flue gas-molten salt heat exchanger 4, a flue gas temperature stabilizer 5 and an electric heater 6 which are heat exchange equipment; the high-temperature salt melting tank 1 and the low-temperature salt melting tank 2 are mainly provided with a cylinder body with a sealing structure, and an electric heating module is arranged on the outer periphery of the cylinder body.
The flue gas temperature stabilizer 5 and the flue gas-molten salt heat exchanger 4 are sequentially arranged in a flue behind the incinerator along the flue gas flow direction, and both take flue gas as an external heat exchange medium and molten salt as an internal heat exchange medium. The internal heat exchange medium of the fused salt-steam reheater 3 is fused salt, the external heat exchange medium is steam from an extraction opening of a steam turbine, and the steam turbine is connected with a generator set of a waste incineration power plant. In the flue gas-molten salt heat exchanger 4, the flue gas is arranged in countercurrent with the molten salt; in the molten salt-steam reheater 3, the molten salt is arranged in countercurrent with steam; in the flue gas temperature stabilizer 5, flue gas and molten salt are arranged downstream; a bypass line is provided between the molten salt inlet and outlet of the flue gas temperature stabilizer 5.
The molten salt outlet arranged at the top of the high-temperature molten salt tank 1 is sequentially connected with a high-temperature molten salt valve 10, a high-temperature molten salt pump 7, a molten salt-steam reheater 3 and a molten salt inlet at the top of the low-temperature molten salt tank 2 through pipelines. Two molten salt outlets are arranged at the bottom of the low-temperature molten salt tank 2, one outlet is sequentially connected with a first low-temperature molten salt valve 11, a first low-temperature molten salt pump 8, a flue gas-molten salt heat exchanger 4, a flue gas temperature stabilizer 5 and a molten salt inlet at the bottom of the high-temperature molten salt tank 1 through pipelines, and the other outlet is sequentially connected with a second low-temperature molten salt valve 12, a second low-temperature molten salt pump 9, an electric heater 6 and a molten salt inlet at the bottom of the high-temperature molten salt tank 1 through pipelines.
In the system, all electric equipment is connected to a power supply system of a garbage incineration power plant through a cable, so that self-power generation supply is realized. The electric heater 6 is also connected to an external power source for consuming surplus electricity through a cable, the external power source being selected from wind power generation equipment, photovoltaic power generation equipment, hydroelectric power generation equipment or a public power grid.
The system can be used for realizing heat storage and electric power consumption of regenerated salt of a waste incineration power plant, and the specific realization method comprises the following steps:
(1) The flue gas at the outlet of the incinerator hearth of the garbage incineration power plant sequentially flows through the flue gas temperature stabilizer 5 and the flue gas-molten salt heat exchanger 4, then continuously flows through the superheater, the economizer and the air preheater, and finally enters the tail gas purification system;
(2) The steam from the steam extraction port of the steam turbine is sent to a fused salt-steam reheater 3 to exchange heat with the fused salt extracted from the high-temperature fused salt tank 1, the high-pressure steam after temperature rise is sent back to the steam turbine to release heat and do work for power generation, and the cooled fused salt is sent to a low-temperature fused salt tank 2;
(3) Molten salt is extracted from the low-temperature molten salt tank 2 and sent to the electric heater 6 and the flue gas-molten salt heat exchanger 4 respectively. The molten salt is heated in the electric heater 6 for taking up the power balance of the power plant or external power supply; the molten salt exchanges heat with the flue gas in a flue gas-molten salt heat exchanger 4 in a countercurrent way and is used for absorbing the waste heat of the flue gas; then continuously sending the mixture into a smoke temperature stabilizer 5 to exchange heat with smoke in concurrent flow for stabilizing the temperature of the smoke; the molten salt which is further warmed up after absorbing the heat is returned to the high-temperature molten salt tank 1 for reducing the non-uniformity of the temperature distribution in the tank.
(4) In the flue gas temperature stabilizer 5, part of molten salt flows back to the inflow port from the outlet through the bypass pipe, and is used for adjusting the flow rate of the molten salt to stabilize the temperature of the flue gas, so that the residence time of the flue gas in a temperature region above 850 ℃ is prolonged to at least 5 seconds, and the decomposition of organic matters including dioxin is promoted;
in the method, the molten salt temperatures in the high-temperature molten salt tank 1 and the low-temperature molten salt tank 2 are controlled to be 850+/-20 ℃ and 600+/-15 ℃ respectively; the temperature of molten salt at the inlet of the smoke temperature stabilizer 5 is 800+/-10 ℃, and the temperature of molten salt at the outlet is 850+/-10 ℃; the molten salt temperatures at the outlets of the flue gas-molten salt heat exchanger 4, the molten salt-steam reheater 3 and the electric heater 6 are respectively consistent with the molten salt temperatures at the corresponding reaching positions. The external heat exchange medium of the smoke temperature stabilizer 5 is smoke at the outlet of the hearth of the incinerator, the temperature of the inlet side is 950+/-50 ℃, and the temperature of the outlet side is 850+/-10 ℃; the external heat exchange medium of the flue gas-molten salt heat exchanger 4 is flue gas from the outlet of the flue gas temperature stabilizer 5, the temperature of the inlet side is 850+/-10 ℃ and the temperature of the outlet side is 650+/-15 ℃; the pipe wall temperature of the electric heater 6 is 950+/-50 ℃; on the steam side of the molten salt-steam reheater 3, the steam parameters at the inlet were 0.6MPa and 248 ℃, and the steam parameters at the outlet were 3.82MPa and 435 ℃.
And controlling the molten salt flow entering the bypass pipelines of the flue gas-molten salt heat exchanger 4, the molten salt-steam reheater 3, the electric heater 6 and the flue gas temperature stabilizer 5 by using valves arranged in the system. Wherein, the flow rate of the molten salt of the flue gas-molten salt heat exchanger 4 is adjusted according to the temperature of the molten salt at the outlet side; the molten salt flow of the molten salt-steam reheater 3 is adjusted according to the steam temperature at the outlet side; the flow rate of the molten salt of the electric heater 6 is regulated according to the temperature of the molten salt at the outlet side; the molten salt flow of the bypass pipeline of the flue gas temperature stabilizer 5 is regulated according to the flue gas temperature at the outlet side.
Specific application examples:
a waste incineration power plant in Zhejiang is selected, and various devices, pumps, valves and pipelines are installed in a power generation device adopting a traditional process according to the figures 1 and 2. The outside of the cylinder bodies of the high-temperature molten salt tank 1 and the low-temperature molten salt tank 2 are provided with fully-enclosed or semi-enclosed electric heating modules which are used for heating molten salt when the machine is stopped or the temperature of the molten salt is too low (the temperature of the high-temperature molten salt is lower than 835 ℃ and the temperature of the low-temperature molten salt is lower than 585 ℃). NaCl-KCl-CaCl serving as an internal heat exchange medium is filled in the high-temperature molten salt tank 1 and the low-temperature molten salt tank 2 2 The melting point of the ternary eutectic chloride salt is 543 ℃ and 1.01X10% 5 The mass loss at 850℃for 5h was 4% at Pa. And then heating is started to melt the molten salt, and equipment testing and preparation for operation are performed after the exhaust.
And the flue gas at the outlet of the incinerator hearth sequentially flows through the flue gas temperature stabilizer 5 and the flue gas-molten salt heat exchanger 4, then continuously flows through other heat exchangers such as a superheater, an economizer, an air preheater and the like, and finally enters the tail gas purification system. High-temperature molten salt is extracted from the high-temperature molten salt tank 1 and sent to the molten salt-steam reheater 3. The steam from the steam turbine is heated by the fused salt-steam reheater 3, the temperature and pressure are increased, and then the steam is used as high-pressure stage steam inlet and is returned to the steam turbine for heat release and work. After the fused salt is extracted from the low-temperature fused salt tank 2, the fused salt flows through the flue gas-fused salt heat exchanger 4 and the flue gas temperature stabilizer 5 in sequence, and the fused salt returns to the high-temperature fused salt tank 1 after absorbing the heat of the flue gas respectively, so as to preserve and reduce the non-uniformity of the fused salt temperature in the tank. The residence time of the flue gas in the high temperature area is prolonged by utilizing the flue gas temperature stabilizer 5, the residence time of the flue gas above 850 ℃ is ensured to be at least 5s, and the pyrolysis of dioxin and other organic matters is promoted. The low-temperature molten salt is pumped out from the low-temperature molten salt tank 2, sent to the electric heater 6 to absorb heat, and then sent to the high-temperature molten salt tank 1.
Table 1 shows the heat transfer medium parameters for each apparatus. The molten salt flow rates of the high-temperature molten salt pump 7, the first low-temperature molten salt pump 8 and the second low-temperature molten salt pump 9 are respectively controlled by corresponding valves, and the adjustment quantity is controlled according to medium temperature feedback. Wherein, the feedback parameter of the flue gas temperature stabilizer 5 and the flue gas-molten salt heat exchanger 4 is the flue gas side outlet temperature, the feedback parameter of the electric heater 6 is the outlet end molten salt temperature, and the feedback parameter of the molten salt-steam reheater 3 is the steam outlet side temperature.
Table 1 heat transfer medium parameters for apparatus
The embodiment is obtained by modifying a waste incineration power plant based on the traditional process, and the daily power generation amount of the original device is 120 kilowatts, and the peak regulation capacity after modification is 25%. The fused salt heat storage material is NaCl-KCl-CaCl 2 50-30-20wt.%, the total amount of molten salt is 3500t, the total heat storage capacity is 175 kilo MJ, 7 kilo watt hours of the generated energy of the power plant can be consumed, and the thermoelectric conversion rate of the molten salt in the heat release process reaches 78%. In addition, the dioxin emission is controlled by 0.0670ng I-TEQ/Nm compared with the prior modification 3 Reduced to 0.0047ng I-TEQ/Nm 3 Reducing the amplitude by 30 percent. Therefore, the invention can truly solve the technical problems in practical applicationCorresponding technical effects are obtained.
The foregoing is a specific embodiment of the present invention, and it will be apparent to those skilled in the art that various applications, additions, modifications and variations can be made to the present invention without departing from the spirit and scope of the invention. If various applications, additions, modifications and variations based on the present invention fall within the scope of the claims and the equivalents thereof, the present invention is also intended to include such applications, additions, modifications and variations.
Claims (10)
1. The electric power consumption system of the waste incineration power plant based on the regenerated salt heat storage of the incineration fly ash is characterized by comprising a high-temperature salt melting tank and a low-temperature salt melting tank which are arranged in the waste incineration power plant, and a smoke temperature stabilizer, a smoke-fused salt heat exchanger, a fused salt-steam reheater and an electric heater which are used as heat exchange equipment; wherein,,
the flue gas temperature stabilizer and the flue gas-molten salt heat exchanger are sequentially arranged in a flue behind the incinerator along the flue gas flow direction, and both take flue gas as an external heat exchange medium and molten salt as an internal heat exchange medium; the internal heat exchange medium of the fused salt-steam reheater is fused salt, the external heat exchange medium is steam from an extraction opening of a steam turbine, and the steam turbine is connected with a generator set of the waste incineration power plant; the fused salt is regenerated salt obtained by water washing, salt leaching and evaporative crystallization of waste incineration fly ash, and has a melting point of less than or equal to 550 ℃ and 1.01X10 5 5h mass loss at Pa and 850 ℃<5, the heat storage operation requirement within the temperature range of 600-850 ℃ can be met;
the molten salt outlet arranged at the top of the high-temperature molten salt tank is sequentially connected with a molten salt pump, a molten salt-steam reheater and a molten salt inlet at the top of the low-temperature molten salt tank through pipelines; two molten salt outlets are arranged at the bottom of the low-temperature molten salt tank, one outlet is sequentially connected with a molten salt pump, a flue gas-molten salt heat exchanger, a flue gas temperature stabilizer and a molten salt inlet at the bottom of the high-temperature molten salt tank through pipelines, and the other outlet is sequentially connected with the molten salt pump, an electric heater and the molten salt inlet at the bottom of the high-temperature molten salt tank through pipelines.
2. The system of claim 1, wherein the bodies of the high temperature molten salt tank and the low temperature molten salt tank are cylinders having a sealed structure, and an electric heating module is disposed around the outside of the cylinders.
3. The system of claim 1, wherein all of the consumers in the system are connected to a power supply system of the waste incineration power plant by cables to achieve self-power generation.
4. The system of claim 1, wherein the electric heater is further connected to an external power source via a cable, the external power source being a wind power plant, a photovoltaic power plant, a hydro power plant, or a utility grid.
5. The system of claim 1, wherein in the flue gas-molten salt heat exchanger, the flue gas is arranged counter-currently to the molten salt; in the molten salt-steam reheater, the molten salt is arranged in countercurrent with steam; in the smoke temperature stabilizer, the smoke and molten salt are arranged in parallel flow; a bypass pipeline is arranged between the molten salt inlet and outlet of the smoke temperature stabilizer.
6. A method for implementing electric power consumption in a waste incineration plant using the system according to claim 1, comprising:
(1) The flue gas at the outlet of the incinerator hearth of the garbage incineration power plant sequentially flows through a flue gas temperature stabilizer and a flue gas-molten salt heat exchanger, and enters a tail gas purification system after exchanging heat with molten salt in the flue gas temperature stabilizer and the flue gas-molten salt heat exchanger;
(2) The steam from the steam extraction port of the steam turbine enters a fused salt-steam reheater to exchange heat with fused salt extracted from a high-temperature fused salt tank, and the warmed steam is sent back to the steam turbine to release heat and do work for power generation; the molten salt after cooling is sent into a low-temperature molten salt tank;
(3) Pumping molten salt from the low-temperature molten salt tank, and respectively sending the molten salt to an electric heater and a flue gas-molten salt heat exchanger; the molten salt is heated in the electric heater for consuming the power allowance of the power plant or external power supply; the molten salt exchanges heat with the flue gas in a flue gas-molten salt heat exchanger in a countercurrent way, and is used for absorbing the waste heat of the flue gas; then continuously sending the mixture into a smoke temperature stabilizer 5 to exchange heat with smoke in concurrent flow for stabilizing the temperature of the smoke; the molten salt which is heated further after absorbing heat is sent back to the high-temperature molten salt tank for reducing the non-uniformity of temperature distribution in the tank;
(4) In the flue gas temperature stabilizer, part of molten salt flows back to the inflow port from the outlet through the bypass pipe, and is used for adjusting the flow rate of the molten salt to stabilize the temperature of flue gas, so that the residence time of the flue gas in a temperature region above 850 ℃ is prolonged to at least 5 seconds, and the decomposition of organic matters including dioxin is promoted.
7. The method of claim 6, wherein the molten salt temperatures in the high temperature molten salt tank and the low temperature molten salt tank are controlled to be 850±20 ℃ and 600±15 ℃, respectively; the temperature of molten salt at the inlet of the smoke temperature stabilizer is 800+/-10 ℃, and the temperature of molten salt at the outlet of the smoke temperature stabilizer is 850+/-10 ℃; the molten salt temperatures at the outlets of the flue gas-molten salt heat exchanger, the molten salt-steam reheater and the electric heater are respectively consistent with the molten salt temperatures at the corresponding reaching positions.
8. The method according to claim 6, wherein the external heat exchange medium of the flue gas temperature stabilizer is flue gas at the outlet of the furnace chamber of the incinerator, and the temperature of the inlet side is 950+/-50 ℃ and the temperature of the outlet side is 850+/-10 ℃; the external heat exchange medium of the flue gas-molten salt heat exchanger is flue gas from the outlet of the flue gas temperature stabilizer, the temperature of the inlet side of the flue gas-molten salt heat exchanger is 850+/-10 ℃, and the temperature of the outlet side of the flue gas-molten salt heat exchanger is 650+/-15 ℃; the temperature of the pipe wall of the electric heater is 950+/-50 ℃; on the steam side of the molten salt-steam reheater, the steam parameters at the inlet are 0.6MPa and 248 ℃, and the steam parameters at the outlet are 3.82MPa and 435 ℃.
9. The method of claim 6, wherein the flow of molten salt into the flue gas-molten salt heat exchanger, the molten salt-steam reheater, the electric heater and the flue gas temperature stabilizer bypass line is controlled by a valve; the flow of molten salt of the flue gas-molten salt heat exchanger is regulated according to the temperature of the molten salt at the outlet side; the molten salt flow of the molten salt-steam reheater is adjusted according to the steam temperature at the outlet side; the molten salt flow of the electric heater is regulated according to the molten salt temperature at the outlet side; and the molten salt flow of the bypass pipeline of the smoke temperature stabilizer is regulated according to the smoke temperature at the outlet side.
10. The system of claim 6, wherein the molten salt is regenerated salt produced by evaporation and crystallization after salt elution of fly ash water from garbage incineration, and the components are NaCl, KCl and CaCl 2 Is a ternary eutectic chloride salt of (2); the melting point of the ternary eutectic chloride salt is less than or equal to 550 ℃ and is 1.01X10 5 5h mass loss at Pa and 850 ℃<5％。
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