CN111351250A - Float glass waste heat recovery method - Google Patents
Float glass waste heat recovery method Download PDFInfo
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- CN111351250A CN111351250A CN201811565102.2A CN201811565102A CN111351250A CN 111351250 A CN111351250 A CN 111351250A CN 201811565102 A CN201811565102 A CN 201811565102A CN 111351250 A CN111351250 A CN 111351250A
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- 239000005329 float glass Substances 0.000 title claims abstract description 59
- 239000002918 waste heat Substances 0.000 title claims abstract description 40
- 238000011084 recovery Methods 0.000 title claims abstract description 29
- 238000000034 method Methods 0.000 title claims abstract description 21
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 342
- 238000001816 cooling Methods 0.000 claims abstract description 32
- 239000000498 cooling water Substances 0.000 claims abstract description 7
- 238000004519 manufacturing process Methods 0.000 claims abstract description 5
- 238000003860 storage Methods 0.000 claims description 48
- 238000009413 insulation Methods 0.000 claims description 9
- 238000005086 pumping Methods 0.000 claims description 5
- 238000009826 distribution Methods 0.000 abstract description 2
- 230000000694 effects Effects 0.000 abstract description 2
- AMXOYNBUYSYVKV-UHFFFAOYSA-M lithium bromide Chemical compound [Li+].[Br-] AMXOYNBUYSYVKV-UHFFFAOYSA-M 0.000 description 130
- 238000010438 heat treatment Methods 0.000 description 35
- 238000005338 heat storage Methods 0.000 description 11
- 230000008859 change Effects 0.000 description 8
- 239000000446 fuel Substances 0.000 description 6
- 239000007789 gas Substances 0.000 description 5
- 238000012546 transfer Methods 0.000 description 5
- 230000008901 benefit Effects 0.000 description 4
- 230000008878 coupling Effects 0.000 description 4
- 238000010168 coupling process Methods 0.000 description 4
- 238000005859 coupling reaction Methods 0.000 description 4
- 238000010248 power generation Methods 0.000 description 4
- 239000002699 waste material Substances 0.000 description 4
- 239000002440 industrial waste Substances 0.000 description 3
- 238000009434 installation Methods 0.000 description 3
- 230000005855 radiation Effects 0.000 description 3
- 238000010586 diagram Methods 0.000 description 2
- 239000012774 insulation material Substances 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 238000013459 approach Methods 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000004146 energy storage Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000020169 heat generation Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 239000008400 supply water Substances 0.000 description 1
- 238000009423 ventilation Methods 0.000 description 1
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Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B15/00—Sorption machines, plants or systems, operating continuously, e.g. absorption type
- F25B15/02—Sorption machines, plants or systems, operating continuously, e.g. absorption type without inert gas
- F25B15/06—Sorption machines, plants or systems, operating continuously, e.g. absorption type without inert gas the refrigerant being water vapour evaporated from a salt solution, e.g. lithium bromide
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
- F01K17/00—Using steam or condensate extracted or exhausted from steam engine plant
- F01K17/02—Using steam or condensate extracted or exhausted from steam engine plant for heating purposes, e.g. industrial, domestic
- F01K17/025—Using steam or condensate extracted or exhausted from steam engine plant for heating purposes, e.g. industrial, domestic in combination with at least one gas turbine, e.g. a combustion gas turbine
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F24—HEATING; RANGES; VENTILATING
- F24D—DOMESTIC- OR SPACE-HEATING SYSTEMS, e.g. CENTRAL HEATING SYSTEMS; DOMESTIC HOT-WATER SUPPLY SYSTEMS; ELEMENTS OR COMPONENTS THEREFOR
- F24D15/00—Other domestic- or space-heating systems
- F24D15/04—Other domestic- or space-heating systems using heat pumps
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B30/00—Heat pumps
- F25B30/04—Heat pumps of the sorption type
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- 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
- F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02B—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO BUILDINGS, e.g. HOUSING, HOUSE APPLIANCES OR RELATED END-USER APPLICATIONS
- Y02B30/00—Energy efficient heating, ventilation or air conditioning [HVAC]
- Y02B30/62—Absorption based systems
- Y02B30/625—Absorption based systems combined with heat or power generation [CHP], e.g. trigeneration
Abstract
A float glass waste heat recovery method belongs to the field of heat supply waste heat recovery and heat distribution, and aims to solve the problem that float glass is used as a low-temperature heat source, circulating water in a cold pool is pressurized by a first circulating pump, a second control valve is opened, the circulating water in the cold pool is conveyed to a float glass workshop to be used as float glass production cooling water, when heat exchange is not needed, an eighth control valve, a ninth control valve, a tenth control valve, an eleventh control valve, a third control valve, a fourth control valve, a fifth control valve and a sixth control valve are opened, a seventh control valve is closed, circulating water at 37-39 ℃ in a hot pool is extracted by a circulating pump of a water supply pipe and is directly extracted to a cooling tower for cooling, the effect is that the temperature of intermediate water is increased, the temperature is reduced after heat exchange, and the intermediate water is conveyed back to a float glass heat exchange machine room, so that a large amount of low.
Description
Technical Field
The invention belongs to the field of heat supply waste heat recovery and heat distribution, and relates to a float glass waste heat recovery method.
Background
In recent years, with the increase of urban heating area and the increase of industrial factory building production line construction in China, the heat consumption in China is rapidly increased, and the heat supply mode is analyzed, so that at present, the heating of residents in China mainly has the following modes: the system comprises a heat and power cogeneration mode, a centralized heating mode of small and medium-sized regional boiler rooms, a household small gas water heater, a household coal-fired furnace and the like, wherein the heat and power cogeneration mode is a comprehensive energy utilization technology for generating power by utilizing high-grade heat energy of fuel and then supplying heat to low-grade heat energy of the fuel. At present, the average power generation efficiency of 300 ten thousand kilowatt thermal power plants in China is 33%, when the thermal power plants supply heat, the power generation efficiency can reach 20%, the rest 80%, more than 70% of heat can be used for supplying heat, 10000 kilojoule of thermal fuel is used, a cogeneration mode is adopted, 2000 kilojoule of power and 7000 kilojoule of heat can be generated, and a common thermal power plant is adopted for power generation, 6000 kilojoule of fuel needs to be consumed by the 2000 kilojoule of power, so that the power generated by the cogeneration mode is deducted from the fuel consumption of the common power plant according to the power generation efficiency of the common power plant, and the rest 4000 kilojoule of fuel can generate 7000 kilojoule of heat. In this sense, the heat supply efficiency of the thermal power plant is 170%, which is about twice of the heat supply efficiency of the small and medium-sized boiler rooms. When the conditions allow, the heating mode of cogeneration should be developed preferentially. In cogeneration heat supply, there are some problems, for example; on one hand, high-temperature steam in a power plant is expensive, on the other hand, a large amount of heat insulation materials are needed in a high-temperature steam heating pipeline to reduce heat loss, and under the condition that the heating temperature is higher, large heat loss can be caused even though more heat insulation materials are used. Therefore, other heat sources such as industrial waste heat with low price and large yield need to be found to replace high-temperature steam in a power plant part. The waste heat of low-temperature industry represented by a float glass plant is abandoned at present, or the extra water and electricity resources are used for emission, so that the waste heat is discarded with the disadvantage.
Disclosure of Invention
In order to solve the problem that float glass is used as a low-temperature heat source, the invention provides the following technical scheme:
a float glass waste heat recovery method comprises the steps that circulating water at 37-39 ℃ generated in a float glass workshop is introduced into a hot pool through a first water pipe, a second circulating pump and a third circulating pump are pressurized, after pressurization is finished, an eighth control valve, a ninth control valve, a tenth control valve and an eleventh control valve are opened, the third control valve, the fourth control valve, the fifth control valve and the sixth control valve are closed, a seventh control valve is opened, the circulating water at 37-39 ℃ in the hot pool is pumped by a circulating pump of a water feeding pipe and is pumped to evaporators in a first heat pump, a second heat pump and a third heat pump to serve as hot end input of the evaporators, the circulating water at 37-39 ℃ exchanges heat with intermediate water at 24-26 ℃ at a cold end of a condenser, after heat exchange, the hot end of the condenser outputs the intermediate water at 33-35 ℃, the cold end of the evaporators outputs the circulating water at 31-33 ℃ to a cooling tower and is supplied to a cooling tower and discharged into a cold pool after being cooled by the cooling tower, and when heat exchange is not needed, opening an eighth control valve, a ninth control valve, a tenth control valve, an eleventh control valve, a third control valve, a fourth control valve, a fifth control valve and a sixth control valve, closing a seventh control valve, and pumping the circulating water at 37-39 ℃ in the hot pool to a circulating pump of a water feeding pipe and directly pumping the circulating water to a cooling tower for cooling.
Furthermore, the hot ends of the condensers of the first heat pump, the second heat pump and the third heat pump output the intermediate water with the temperature of 33-35 ℃ and are collected by the water collector.
Furthermore, a fourth circulating pump for pumping intermediate water in the water collector is installed on a pipeline at the front end of the collector, and the front end of the fourth circulating pump is connected with the water storage tank.
Furthermore, the intermediate water at 24-26 ℃ at the cold ends of the condensers of the first heat pump, the second heat pump and the third heat pump is supplied by the first water separator.
Further, in the power-off state, the second control valve is closed, the first control valve is opened, and the water in the preparation water tank can provide 15 minutes of cooling water for the float glass workshop.
Furthermore, the hot pond and the cold pond are separated by a heat insulation layer, the heat insulation layer is provided with overflow ports communicated with the two ponds, and water in the hot pond or the cold pond is excessive and exceeds the overflow ports to enter the corresponding pond, so that the water is not directly overflowed from the pond due to excessive water stored in the single pond.
Has the advantages that: a heat exchange machine room is built in a float glass plant area, industrial waste heat in circulating water of a cooling tower of the float glass plant area is cooled through a heat exchanger in winter, the temperature of intermediate water is raised, the temperature is reduced after heat exchange, and the intermediate water is conveyed back to the float glass heat exchange machine room, so that a large amount of low-temperature heat sources are obtained.
Drawings
FIG. 1 is a piping connection diagram of the apparatus of the present invention.
Fig. 2 is a piping connection diagram of the cogeneration unit of the power plant of the present invention.
1. A float glass workshop, 2, a prepared water tank, 3, a first control valve, 4, a second control valve, 5, a first circulating pump, 6, a cooling tower, 7, a third control valve, 8, a fourth control valve, 9, a fifth control valve, 10, a sixth control valve, 11, a seventh control valve, 12, an eighth control valve, 13, a ninth control valve, 14, a tenth control valve, 15, an eleventh control valve, 16, a twelfth control valve, 17, a second circulating pump, 18, a third circulating pump, 19, an overflow port, 20, a heat insulation layer, 21, a cold pool, 22, a hot pool, 23, a first heat pump, 24, a second heat pump, 25, a third heat pump, 26, a water collector, 27, a fourth circulating pump, 28, a first water separator, 29, a temperature sensor, 30, a fifth circulating pump, 31, a phase change heat storage device, 32, a thirteenth control valve, 33, a fourteenth control valve, 34, solar water heater, 35. the system comprises a fifteenth control valve, 36, a sixteenth control valve, 37, a seventeenth control valve, 38, a second water divider, 39, a water storage tank, 40, a lithium bromide heat pump, 41, a user end pipeline, 42, a fourth heat pump, 43, a plate heat exchanger, 44, a cogeneration device, 45, a power plant condensed gas return pipe, 46, a sixth circulating pump, 47, and a lithium bromide heat pump high-temperature heat source water outlet end.
1-1, a steam heat pump unit, 1-2, a third lithium bromide heat pump unit, 1-3, a second lithium bromide heat pump unit, 1-4, a first lithium bromide heat pump unit, 1-5, a steam-water heat exchanger, 1-6, a steam exhaust device and 1-7, a steam turbine.
Detailed Description
Example 1: an integrated multi-waste-heat coupling heating system comprises a float glass waste heat recovery device, a solar waste heat recovery device and a lithium bromide heat pump heating device.
Float glass waste heat recovery device, including float glass workshop (1), hot pond (22), cold pond (21), second circulating pump (17), third circulating pump (18) two-stage control valve, cooling tower (6), heat pump, the first delivery port of float glass workshop (1) lets in hot pond (22) by first water pipe, the entry intercommunication water-supply pipe of cooling tower (6), the outlet line of cooling tower (6) lets in cold pond (21), water-supply pipe installation two-stage control valve and circulating pump, water-supply pipe lets in hot pond (22), the circulating pump sets up the position department between hot pond (22) and the two-stage control valve of water-supply pipe, by between the valve of two-stage control valve the water-supply pipe intercommunication, and be located this part's water-supply pipe intercommunication branch water pipe, branch water pipe is by the tube coupling heat pump, and be located this part's pipeline and install seventh control valve (11).
The heat pump comprises three groups, namely a heat pump 23, a heat pump 24 and a heat pump 25, wherein the hot end input of the evaporator of each heat pump (23, 24, 25) is a branch water pipe, and the cold end output of the evaporator of each heat pump is connected with a cooling tower (6). And a twelfth control valve (16) is arranged on a communication pipeline between the cold end output of the evaporator of the heat pump and the cooling tower (6). The hot end output of the condenser of the heat pump (23, 24, 25) is a water collector (26), a fourth circulating pump (27) is installed on a front end pipeline of the water collector (26), the front end of the fourth circulating pump (27) is communicated with a circulating water inlet of a water storage tank (39) of the solar waste heat recovery device, the cold end input of the condenser of the heat pump (23, 24, 25) is a first water divider (28), and the first water divider (28) is connected with an outlet of a low-temperature heat exchange section of the lithium bromide heat pump heating device.
The inlet of the cooling tower (6) is connected with the water feeding pipe in parallel at least, a group of control valve groups are installed on each water feeding pipe, each group of control valve groups at least comprises two-way parallel two-stage control valves, the valves of each two-stage control valves are communicated with each other through the water feeding pipe, the water feeding pipes located on the part are communicated with branch water pipes, the branch water pipes are connected with a plurality of paths of heat pumps in parallel through pipelines, and the pipelines located on the part are provided with seventh control valves (11). Specifically, the water feeding pipe comprises a first road water feeding pipe and a second road water feeding pipe which are connected in parallel, the first road water feeding pipe is provided with a first group of control valve sets, the first group of control valve sets comprise a first road two-stage control valve and a second road two-stage control valve which are connected in parallel, the first road two-stage control valve comprises an eighth control valve (12) and a third control valve (7), and the second road two-stage control valve comprises a ninth control valve (13) and a fourth control valve (8); a second group of control valve sets are installed on the second water supply pipe, each second group of control valve sets comprises a first two-stage control valve and a second two-stage control valve which are connected in parallel, each first two-stage control valve comprises a tenth control valve (14) and a fifth control valve (9), and each second two-stage control valve comprises an eleventh control valve (15) and a sixth control valve (10); the heat pump comprises a first heat pump (23), a second heat pump (24) and a third heat pump (25).
Float glass waste heat recovery device still includes prepares water tank (2), the outlet pipe of preparing water tank (2) lets in cold pool (21), the second delivery port intercommunication second water pipe in float glass workshop (1), the second outlet pipe with prepare the outlet pipe intercommunication of water tank (2), the second water pipe both sides the outlet pipe, one side installation first control valve (3), opposite side installation second control valve (4), install first circulating pump (5) on the outlet pipe of second control valve (4) low reaches. The hot pool (22) and the cold pool (21) are separated by a heat insulation layer (20), and an overflow gap (19) communicated with the two pools is arranged on the heat insulation layer (20).
The execution method of the device comprises the following steps: a float glass waste heat recovery method comprises the steps that circulating water at 37-39 ℃ generated in a float glass workshop (1) is introduced into a hot pool (22) through a first water pipe, a second circulating pump (17) and a third circulating pump (18) are pressurized, after pressurization is finished, an eighth control valve (12), a ninth control valve (13), a tenth control valve (14) and an eleventh control valve (15) are opened, a third control valve (7), a fourth control valve (8), a fifth control valve (9) and a sixth control valve (10) are closed, a seventh control valve (11) is opened, the circulating water at 37-39 ℃ in the hot pool (22) is extracted by the circulating pump of a water supply pipe and is extracted to evaporators in a first heat pump (23), a second heat pump (24) and a third heat pump (25) to serve as the hot end input of the evaporators, the circulating water at 37-39 ℃ exchanges heat with intermediate water at 24-26 ℃ at the cold end of a condenser, after heat exchange, the hot end of the condenser outputs medium water with the temperature of 33-35 ℃, the cold end of the evaporator outputs circulating water with the temperature of 31-33 ℃ and the circulating water is supplied to a cooling tower (6), and is discharged into a cold pool (21) after being cooled by a cooling tower (6), the circulating water of the cold pool (21) is pressurized by a first circulating pump (5), a second control valve (4) is opened, the circulating water of the cold pool (21) is conveyed to a float glass workshop (1) to be used as cooling water for float glass production, when heat exchange is not needed, opening an eighth control valve (12), a ninth control valve (13), a tenth control valve (14), an eleventh control valve (15), a third control valve (7), a fourth control valve (8), a fifth control valve (9) and a sixth control valve (10), and the seventh control valve (11) is closed, and circulating water at 37-39 ℃ in the hot pool (22) is pumped by a circulating pump of the water feeding pipe and is directly pumped to the cooling tower (6) for cooling. The cold end of the evaporator outputs circulating water with the temperature of about 31-33 ℃ and supplies the circulating water to the cooling tower (6), the temperature of the cooling water in the process flow production is required to be 20-30 ℃, namely the temperature of the water in the cold pool (21) is kept in a relatively stable temperature environment of 20-30 ℃, if the temperature of the circulating water output by the cold end of the evaporator is higher than 30 ℃, the circulating water is cooled by the cooling tower (6) and then discharged into the cold pool (21), and if the temperature of the circulating water output by the cold end of the evaporator is lower than 30 ℃, the circulating water is directly discharged into the cold pool (21) through the cooling tower (6).
The hot ends of the condensers of the first heat pump (23), the second heat pump (24) and the third heat pump (25) output the intermediate water with the temperature of 33-35 ℃ and are collected by a water collector (26). The pipeline of the front end of the water collector is provided with a fourth circulating pump (27) used for pumping intermediate water in the water collector (26), and the front end of the fourth circulating pump is connected with a water storage tank (39) of the solar waste heat recovery device. The intermediate water of 24-26 ℃ input from the cold ends of the condensers of the first heat pump (23), the second heat pump (24) and the third heat pump (25) is supplied by a first water separator (28), the first water separator (28) is connected with the outlet of the low-temperature heat exchange section of the lithium bromide heat pump heating device, the heat exchange water of the low-temperature heat exchange section is used as the intermediate water of 24-26 ℃, the intermediate water for float glass waste heat recovery is reheated by the solar waste heat recovery device, part of heat and high-temperature hot water of a power plant are subjected to heat exchange for a user pipeline in the lithium bromide heat pump heating device, the float glass waste heat and the solar waste heat are used as heating heat sources, the intermediate water with relatively stable low temperature after heat exchange is used for cold end output of the condenser of the heat pump unit, the intermediate water is circulated and participates in heat exchange, and the water quantity and the heat are saved.
In the power-off state, the second control valve (4) is closed, the first control valve (3) is opened, and the water in the prepared water tank (2) can provide cooling water for the float glass workshop (1) for 15 minutes. The hot pond (22) and the cold pond (21) are separated by a heat insulation layer (20), the heat insulation layer (20) is provided with an overflow port (19) for communicating the two ponds, and water in the hot pond (22) or the cold pond (21) is excessive and exceeds the overflow port (19) to enter the corresponding pond, so that the water is not directly overflowed from the pond due to excessive water in the single pond.
The solar waste heat recovery device comprises a solar water heater (34), a phase change heat storage device (31), a water storage tank (39), a temperature sensor (29), a fifth circulating pump (30), a thirteenth control valve (32), a fourteenth control valve (33) and a fifteenth control valve (35), wherein a circulating outlet of the water storage tank (39) is connected with the solar water heater (34) through a pipeline, a fifteenth control valve (35) is arranged on the pipeline section, a water outlet pipe of the solar water heater (34) is branched into two parallel water pipes, a thirteenth control valve (32) is arranged on one water pipe, and is connected with the fifth circulating pump (30), a fourteenth control valve (33) is arranged on the other water pipe, and is connected with a phase change heat storage device (31), the phase change heat storage device (31) is connected with the fifth circulating pump (30), and the outlet of the fifth circulating pump (30) is connected with the circulating inlet of the water storage tank (39). The inlet of the water storage tank (39) is connected with a water collector (26), the water collector (26) is the water collector (26) of the float glass waste heat recovery device, and the water collector (26) is connected with the high-temperature output ends of the condensers of the three groups of heat pumps of the float glass waste heat recovery device.
The water storage tank (39) is connected with the second water divider (38) through a heat exchange pipeline, a heat exchange section of the heat exchange pipeline is located inside the water storage tank (39), the second water divider (38) is arranged on the cogeneration device (44), and the cogeneration device (44) is connected to an inlet of a high-temperature section of the lithium bromide heat pump heating device through the second water divider (38). The outlet of the water storage tank (39) is connected to the inlet of the low-temperature heat exchange section of the lithium bromide heat pump heating device through a pipeline. A seventeenth control valve (37) is arranged on the water supply pipeline connected with the outlet of the water storage tank (39) and is used for controlling the water quantity and the speed of the solar waste heat recovery device for supplying the stored water to the lithium bromide heat pump heating device. The cogeneration unit (44) is connected to a power plant, wherein the steam temperature is about 100 ℃, the temperature of the water output from the water storage tank (39) is about 45 ℃, and the temperature of the water output from the water storage tank (39) is maintained at about 45 ℃ by a heat exchange section in which the second water separator (38) is connected to the water storage tank (39). A temperature sensor (29) is installed in the water storage tank (39) to measure the temperature of the stored water.
The execution method of the device comprises the following steps: a method for recovering the waste heat of solar energy,
and (3) a normal mode: when the solar radiation intensity is relatively moderate, i.e. when day 7: 00 to day 11: 00 and day 15: 00 to day 19: when the temperature is 00 hours, opening a fifteenth control valve (35), closing a fourteenth control valve (33), opening a thirteenth control valve (32), so that water in a water storage tank (39) is extracted from a circulating outlet of the water storage tank (39) by a fifth circulating pump (30), the water in the water storage tank (39) is heated by a solar water heater (34), the heated water is directly extracted to the water storage tank (39) through a pipeline provided with the thirteenth control valve (32), and the heated water flows back to the water storage tank (39) from a circulating water inlet of the water storage tank (39); circulating the stored water heating cycle until the mode is changed or the measured value of the temperature sensor (29) in the water storage tank (39) reaches a set threshold value;
and (3) energy storage mode: when the intensity of solar radiation is relatively excessive, i.e. when day 11: 00 to 15: when the temperature is 00 hours, opening a fifteenth control valve (35), closing a thirteenth control valve (32), opening a fourteenth control valve (33), starting a phase change heat storage device (31), enabling water in a water storage tank (39) to be extracted from a circulating outlet of the water storage tank (39) by a fifth circulating pump (30), heating the water in the water storage tank (39) by a solar water heater (34), and enabling the phase change heat storage device (31) to store excessive heat energy through a pipeline provided with the phase change heat storage device (31) so as to keep the outlet water temperature at a set temperature; circulating the water storage heating circulation until the mode is changed;
a heat generation mode: when the intensity of solar radiation is relatively insufficient, i.e. when the day 19: 00 to the next day 7: 00 hours or when the temperature sensor (29) measures that the water temperature is continuously lower than 40 ℃ within half an hour; closing the thirteenth control valve (32), opening the fourteenth control valve (33), starting the phase-change heat storage device (31), so that water in the water storage tank (39) is pumped out by the fifth circulating pump (30) from a circulating outlet of the water storage tank (39), the water in the water storage tank (39) is heated by the solar water heater (34), and heat energy stored in a heat storage mode is released by the phase-change heat storage device (31) through a pipeline provided with the phase-change heat storage device (31), so that the outlet water temperature is increased and kept at the set temperature; and circulating the stored water heating circulation until the mode is changed.
In the three modes, the inlet of the water storage tank (39) is communicated with the water collector (26) to supply water to the water storage tank (39). And an outlet of the water storage tank (39) is communicated with a low-temperature heat exchange section of the lithium bromide heat pump (40) and is used for conveying low-temperature heat exchange water. The low temperature heat transfer water was 45 ℃.
The lithium bromide heat pump heating device comprises a lithium bromide heat pump (40), a plate heat exchanger (43) and a fourth heat pump (42); the lithium bromide heat pump (40) comprises a high-temperature heat exchange section, a low-temperature heat exchange section and a medium-temperature heat exchange section; the inlet of the high-temperature heat exchange section is connected with a cogeneration device (44), the outlet of the high-temperature heat exchange section is connected with a high-temperature heat exchange water pipe of a plate heat exchanger (43), the inlet of the low-temperature heat exchange section is connected with a water supply pipe, the outlet of the low-temperature heat exchange section is connected with a first output pipeline, and the intermediate-temperature heat exchange section is connected with a second output pipeline; the plate heat exchanger (43) comprises a high-temperature heat exchange water pipe and a low-temperature heat exchange water pipe, the outlet of the high-temperature heat exchange water pipe is connected with the hot end of the evaporator of the fourth heat pump (42), and the low-temperature heat exchange water pipe is connected with the third output pipeline; and the cold end output of the evaporator of the fourth heat pump (42) is connected with a power plant condensed gas return pipe (45), and the hot end output of the condenser of the heat pump is connected with a fourth output pipeline. And the heat and power cogeneration device (44) is connected with an inlet of the high-temperature heat exchange section, is communicated with the high-temperature heat exchange section of the lithium bromide heat pump (40) and conveys high-temperature heat exchange water to the high-temperature heat exchange section, the second water divider (38) is connected with the water storage tank (39) through a heat exchange pipeline, and the heat exchange section of the heat exchange pipeline is positioned inside the water storage tank (39). An inlet of the low-temperature heat exchange section is connected with a water supply pipe, and the water supply pipe is connected with an outlet of the water storage tank (39). The first output pipeline is connected with a first water distributor (28), the water distributor is connected to the cold end of a condenser of the heat pump (23, 24, 25), and a sixth circulating pump (46) is installed on the connecting pipeline of the output pipeline and the first water distributor (28). The second output pipeline, the third output pipeline and the fourth output pipeline are connected with the user side pipeline and output in a grading mode. The cogeneration device (44) is connected to a power plant, the temperature of steam in the cogeneration device is about 100 ℃, the temperature of water output from the water storage tank (39) is about 45 ℃, and the temperature of the water output from the water storage tank (39) is about 45 ℃ maintained by a heat exchange section of which the water separator is connected with the water storage tank (39); the input temperature of a high-temperature heat exchange section of a lithium bromide heat pump (40) is about 100 ℃, the output temperature is about 60 ℃, the input temperature of a low-temperature heat exchange section is about 45 ℃, the output temperature is about 24-26 ℃, and the output temperature of a medium-temperature heat exchange section is about 55 ℃; the input temperature of a high-temperature heat exchange water pipe of the plate heat exchanger (43) is about 60 ℃, the output temperature is 28-32 ℃, and the output temperature of a low-temperature heat exchange water pipe is about 55 ℃; the input temperature of the hot end of the evaporator of the heat pump is 28-32 ℃, the output temperature is about 5 ℃, and the output temperature of the condenser is about 40-42 ℃.
By the aforesaid, lithium bromide heat pump heating system is to the storage water, carried out the heat transfer between user side and the power plant water, with the heat supply user side of high temperature power plant water and storage water, accomplish the heat transfer through the lithium bromide heat pump promptly, and return power plant and first water knockout drum respectively with the low temperature moisture after the heat transfer, make the low temperature water after the heat transfer continue to participate in the circulation, not only accomplished high temperature heat and low temperature thermal output in the lump, still by cyclic utilization with water, realized water source and thermal saving and make full use of. And in order to be able to directly adapt the low-temperature water to the lithium bromide heat pump, a solar energy waste heat recovery device is added between the float glass waste heat recovery device and the lithium bromide heat pump heating device so as to supplement partial heat with clean energy.
The implementation method of the device is as follows, a lithium bromide heat pump heating method, a condenser lead-in pipe of a power plant is communicated with a high-temperature heat exchange section of a lithium bromide heat pump (40) and conveys high-temperature heat exchange water (100 ℃) to the high-temperature heat exchange section, an outlet of a water storage tank (39) is communicated with a low-temperature heat exchange section of the lithium bromide heat pump (40) and conveys low-temperature heat exchange water (45 ℃) to the low-temperature heat exchange section, and water in the high-temperature heat exchange section, the low-temperature heat exchange section and a medium-temperature heat exchange section exchanges heat so that the medium-temperature heat exchange; the output of the low-temperature heat exchange section is communicated with a first water divider (28) and conveys low-temperature water (25 ℃) to the first water divider;
an output pipeline of the high-temperature heat exchange section is communicated with a high-temperature heat exchange water pipe of the plate heat exchanger (43), and heat exchange water (60 ℃) subjected to heat exchange in the high-temperature heat exchange section is conveyed to the high-temperature heat exchange water pipe, so that the high-temperature heat exchange water pipe exchanges heat with water in the low-temperature heat exchange water pipe, and the low-temperature heat exchange water pipe outputs medium-temperature water (55 ℃) to be supplied to a client;
the output of a high-temperature heat exchange water pipe of the plate heat exchanger (43) is communicated with the hot end input of an evaporator of the fourth heat pump (42), heat exchange water (28-32 ℃) subjected to heat exchange through the high-temperature heat exchange water pipe is conveyed to the heat exchange water pipe, the cold end output of the evaporator of the heat pump is connected with a condenser return water pipe of a power plant, condensate water (5 ℃) is provided for the condenser return water pipe, and the evaporator exchanges heat with water in the condenser so that the hot end of the condenser outputs low-temperature water (34-36 ℃) to be supplied to a client.
And a second water divider (38) arranged on the cogeneration device (44) connected with the inlet of the high-temperature heat exchange section, and used for exchanging heat between high-temperature heat exchange water (100 ℃) and low-temperature heat exchange water in the water storage tank (39) and supplying heat to the low-temperature heat exchange water (45 ℃) in the water storage tank (39).
The cogeneration device of the power plant in the scheme comprises exhaust steam devices (1-6), steam turbines (1-7), steam heat pump units (1-1), third lithium bromide heat pump units (1-2), second lithium bromide heat pump units (1-3) and first lithium bromide heat pump units (1-4), wherein each lithium bromide heat pump unit comprises a high-temperature heat source, a low-temperature heat source and a medium-temperature heat source, the heat exchange pipelines of the exhaust steam devices (1-6) are communicated with the evaporator of the steam heat pump units (1-1) and the low-temperature heat source of each lithium bromide heat pump unit in parallel, the heat exchange pipelines of the steam turbines (1-7) are communicated with the high-temperature heat sources of each lithium bromide heat pump unit in parallel, the high-temperature water outlets of condensers are communicated with the medium-temperature inlets of the first lithium bromide heat pump units (1-4), the outlet of the first lithium bromide heat pump unit (1-4) is communicated with the inlet of the medium-temperature heat source of the second lithium bromide heat pump unit (1-3), and the outlet of the medium-temperature heat source of the second lithium bromide heat pump unit (1-3) is communicated with the inlet of the medium-temperature heat source of the third lithium bromide heat pump unit (1-2).
An inlet of the steam exhaust device (1-6) is connected with an inlet pipe, an outlet of the steam exhaust device is connected with an outlet pipe, the inlet pipe and the outlet pipe are arranged in parallel, the inlet pipe is communicated with an outlet of a low-temperature heat source of the first lithium bromide heat pump unit (1-4), the outlet pipe is communicated with an inlet of a low-temperature heat source of the first lithium bromide heat pump unit (1-4), an inlet of a low-temperature heat source of the second lithium bromide heat pump unit (1-3) is connected into the outlet pipe in parallel, an outlet of the low-temperature heat source of the second lithium bromide heat pump unit (1-3) is connected into the inlet pipe in parallel, an inlet of a low-temperature heat source of the third lithium bromide heat pump unit (1-2) is connected into the outlet pipe in parallel, an outlet; the inlet of the steam turbine (1-7) is connected with an inlet pipe, the outlet of the steam turbine is connected with an outlet pipe, the inlet pipe and the outlet pipe are arranged in parallel, the inlet pipe is communicated with the steam outlet of the steam-water heat exchanger (1-5), the outlet pipe is communicated with the steam inlet of the steam-water heat exchanger (1-5), the inlet of the high-temperature heat source of the first lithium bromide heat pump unit (1-4) is connected into the outlet pipe in parallel, the outlet of the high-temperature heat source of the second lithium bromide heat pump unit (1-3) is connected into the inlet pipe in parallel, the outlet of the high-temperature heat source of the third lithium bromide heat pump unit (1-2) is connected into the outlet pipe in parallel, the outlet of the high-temperature heat source of the third lithium bromide heat pump unit (1-2) is connected into, the outlet of the evaporator of the steam heat pump unit (1-1) is connected with the inlet pipe.
The low-temperature water inlet of the condenser of the steam heat pump unit (1-1) is connected with a water inlet pipeline (about 5 degrees).
And a low-temperature heat source of the third lithium bromide heat pump unit (1-2) is also connected with a water inlet pipeline (about 25 degrees).
The execution method of the cogeneration device of the power plant comprises the following steps: the method comprises the following steps that power plant water with the temperature of about 5 ℃ enters a cold water inlet of a condenser of a steam heat pump unit (1-1), waste steam water generated by a waste steam device (1-6) exchanges heat with the power plant water with the temperature of about 5 ℃ at an evaporator end of the steam heat pump unit (1-1), primary heat exchange water with the temperature of about 30 ℃ is output from a condenser end of the steam heat pump unit (1-1), and the primary heat exchange water enters an intermediate temperature heat source of a first lithium bromide heat pump unit (1-4) and serves as inlet water of the first lithium bromide heat pump unit; waste steam water generated by the waste steam devices (1-6) enters a first lithium bromide heat pump unit (1-4) to be used as a low-temperature heat source, high-temperature steam with the temperature of 100 ℃ generated by a steam turbine (1-7) enters the first lithium bromide heat pump unit (1-4) to be used as a high-temperature heat source, and secondary heat exchange water with the temperature of about 50 ℃ is discharged from a medium-temperature heat source of the first lithium bromide heat pump unit (1-4); the dead steam water generated by the dead steam device (1-6) enters a second lithium bromide heat pump unit (1-3) to be used as a low-temperature heat source, the high-temperature steam generated by the steam turbine (1-7) enters the second lithium bromide heat pump unit (1-3) to be used as a high-temperature heat source, and the effluent water of the medium-temperature heat source of the second lithium bromide heat pump unit (1-3) is three-stage heat exchange water at about 70 ℃; the dead steam water generated by the dead steam device (1-6) enters a third lithium bromide heat pump unit (1-2) to be used as a low-temperature heat source, the high-temperature steam generated by a steam turbine (1-7) enters the third lithium bromide heat pump unit (1-2) to be used as a high-temperature heat source, the effluent water of the medium-temperature heat source of the third lithium bromide heat pump unit (1-2) is four-stage heat exchange water at about 90 ℃, the four-stage heat exchange water enters a steam-water heat exchanger (1-5) to exchange heat with the high-temperature steam generated by the steam turbine (1-7), and the steam-water heat exchanger (1-5) outputs hot water at 100 ℃.
The client is a user heating pipeline. The low-temperature water (25 ℃) received by the first water separator (28) is conveyed to the cold ends of the condensers of the first heat pump (23), the second heat pump (24) and the third heat pump (25) to be used as intermediate water.
The embodiment provides a heating system is united in coupling of high-temperature steam of power plant and low temperature waste heat that float glass factory produced, both can satisfy the heat supply demand and reduce the use of power plant high-temperature steam again, reduces the heating cost by a wide margin.
A heat exchange machine room is built in a float glass plant area, industrial waste heat (38 ℃) in circulating water of a cooling tower in the float glass plant area is cooled to 32 ℃ through a heat exchanger in winter, the temperature of intermediate water is raised to 35 ℃ from 25 ℃, the temperature is reduced to 31-33 ℃ after heat exchange, and the intermediate water is conveyed back to the float glass heat exchange machine room, so that a large amount of low-temperature heat sources are obtained. The low-temperature waste heat generated by the float glass has the following advantages:
the heating and ventilation system is not changed: only the pipeline part of the cooling tower is modified, and other systems are not affected.
The electric power operation cost is not increased: and a heat exchanger machine room is additionally arranged in a plant area, and a cooling tower does not run in a heating season, so that the electric charge is saved.
The other side equipment is not increased or decreased: the cooling tower is not cancelled, and the device can be continuously used in non-heating seasons without influencing other equipment.
The working temperature is not changed: the temperature of the heat exchanger is kept at 32 ℃ after heat exchange, the use requirement is not influenced, and the energy consumption is not increased.
By adopting the scheme, a large amount of waste heat can be recovered without changing the original operation condition of a factory, increasing the power consumption and influencing the product yield. The technical scheme of this embodiment can provide the high-temperature steam coupling heat supply that a large amount of low temperature heat sources and power plant provided, under the condition that does not influence the heat supply effect, greatly reduced the quantity of power plant's high-temperature steam, make full use of the low temperature heat source that float glass factory produced again, reduced the heat supply cost, improved economic benefits. Therefore, the invention has the function of not underestimating the target of energy conservation and emission reduction.
The working condition of a float glass plant is relatively stable, the overhaul time is short, and the following two control modes are provided for the small heat during overhaul:
and (3) a normal mode: under normal operating conditions in a float glass plant, the system operates in all of the above-described ways.
The maintenance mode is as follows: when the maintenance is carried out in a float glass plant, the temperature of water in the water storage tank 39 is lower, under the condition, the heat and power cogeneration device 44 increases the water inflow, the sixteenth control valve 36 is opened, the second water separator 38 separates a certain amount of water to heat the water in the water storage tank 39, so that the water reaches the designed working condition temperature, and the outlet water temperature is 95-100 ℃ and can be used as a high-temperature heat source of the lithium bromide heat pump.
The lithium bromide heat pump heating device comprises a cogeneration device 44, a lithium bromide heat pump 40, a plate heat exchanger 43, a heat pump 42, a user side pipeline 41, a water separator 38, a control valve 36, a power plant condensed gas return pipe 45, a lithium bromide heat pump high-temperature heat source water outlet end 47 and a circulating pump 46. The main working principle is as follows: high-temperature steam at about 100 ℃ is introduced into the power plant from the water return pipe 44 to serve as a high-temperature heat source of the lithium bromide heat pump 40; the lithium bromide heat pump high-temperature heat source water outlet end water (about 60 ℃) enters a plate heat exchanger 43 to exchange heat with a user end pipeline 41 to obtain 55 ℃ hot water for users, the 28-32 ℃ water obtained after heat exchange is subjected to heat exchange through a heat pump 42, the water outlet temperature is about 5 ℃, and the water is sent to a power plant condensed gas return pipe 45 to be sent back to the power plant. The intermediate water with the temperature of 44-45 ℃ and the obtained float glass waste heat enters a low-temperature heat source end of the lithium bromide heat pump 40 through the control valve 37, the outlet water temperature is about 24-26 ℃, and the intermediate water is pressurized by the circulating pump 46 and is sent to the water separator 28 to complete intermediate water circulation. The outlet water temperature of the user end pipeline is 34-36 ℃, and the return water temperature is 54-55 ℃. On the other hand, the low-quality heat of float glass and solar energy and the high-quality heat of steam of a power plant are used as heat sources, and the heat exchange means ensures that the low-quality heat can not be used uselessly, the energy is extremely used, and the step energy is also utilized. In the process, for the heat of the cogeneration device and the float glass, the cold quantity is used once in the recycling of the low-temperature water after heat exchange, the recycling of the circulating water is realized, and the water resource is saved. When the high-temperature steam of the power plant is used, the heat quality of the cogeneration device is gradually improved so as to form high-temperature water suitable for heat exchange, and the temperature of the high-temperature water can reach or approach 100 ℃.
During the heating in winter, the operation is carried out according to the mode, during the non-heating period, the twelfth control valve 16 and the seventh control valve 11 are closed, the water with the temperature of 37-39 ℃ in the float glass hot pool 22 is cooled to 31-33 ℃ in the cooling tower 6 and then is sent into the cold pool 21, and the cooling tower can be controlled and adjusted by opening and closing the third control valve 7, the fourth control valve 8, the fifth control valve 9, the sixth control valve 10, the eighth control valve 12, the ninth control valve 13, the tenth control valve 14 and the eleventh control valve 15.
In the aspect of price, the condensate water of the power plant is expensive, the float glass water is low in price, the water of the power plant is only used as a high-temperature heat source of the lithium bromide heat pump, and the intermediate water obtained by the waste heat of the float glass is used as a low-temperature heat source. Greatly reduces the water consumption of the power plant and improves the economic benefit. The power plant water and the intermediate water obtained from float glass waste heat recovery are not mixed, the power plant water is clean, the intermediate water possibly contains impurities due to overlong obtained pipe, the power plant water is possibly polluted, and the reliability of the system is guaranteed by the use mode of not mixing water. The system integrally uses three sets of heating devices, so that the reliability of heating is greatly improved, and the important civil problem of stable heating is guaranteed.
In one embodiment, any temperature in this application, using a non-exact representation of the temperature around or about or equivalent to the temperature, is defined, such as around 45 ℃ or about 45 ℃, then represents an interval of ± 1 degree of the temperature, i.e. 44-46 ℃ for example, and the specific temperature value directly represents its numerical temperature, whereas in a further preferred embodiment, a direct numerical representation of the temperature referred to in this application is understood to be an interval of ± 1 degree of its temperature, such as 45 degrees of water for heat exchange, representing 44-46 ℃ for example, except with hot water that must be represented by the numerical value, e.g. 100 ℃.
The above description is only for the purpose of creating a preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art can substitute or change the technical solution and the inventive concept of the present invention within the technical scope of the present invention.
Claims (6)
1. A float glass waste heat recovery method is characterized in that circulating water at 37-39 ℃ generated in a float glass workshop (1) is introduced into a hot pool (22) through a first water pipe, a second circulating pump (17) and a third circulating pump (18) are pressurized, after pressurization is finished, an eighth control valve (12), a ninth control valve (13), a tenth control valve (14) and an eleventh control valve (15) are opened, a third control valve (7), a fourth control valve (8), a fifth control valve (9) and a sixth control valve (10) are closed, a seventh control valve (11) is opened, the circulating water at 37-39 ℃ in the hot pool (22) is pumped by the circulating pump of a water supply pipe and is pumped to evaporators in a first heat pump (23), a second heat pump (24) and a third heat pump (25) to be used as the hot end input of the evaporators, the circulating water at 37-39 ℃ is subjected to heat exchange with intermediate heat water at 24-26 ℃ at the cold end of a condenser, after heat exchange, the hot end of the condenser outputs medium water with the temperature of 33-35 ℃, the cold end of the evaporator outputs circulating water with the temperature of 31-33 ℃ and the circulating water is supplied to a cooling tower (6), and is discharged into a cold pool (21) after being cooled by a cooling tower (6), the circulating water of the cold pool (21) is pressurized by a first circulating pump (5), a second control valve (4) is opened, the circulating water of the cold pool (21) is conveyed to a float glass workshop (1) to be used as cooling water for float glass production, when heat exchange is not needed, opening an eighth control valve (12), a ninth control valve (13), a tenth control valve (14), an eleventh control valve (15), a third control valve (7), a fourth control valve (8), a fifth control valve (9) and a sixth control valve (10), and the seventh control valve (11) is closed, and circulating water at 37-39 ℃ in the hot pool (22) is pumped by a circulating pump of the water feeding pipe and is directly pumped to the cooling tower (6) for cooling.
2. The float glass waste heat recovery method according to claim 1, wherein the intermediate water at 33-35 ℃ is output from the hot ends of the condensers of the first heat pump (23), the second heat pump (24) and the third heat pump (25) and is collected by a water collector (26).
3. The float glass waste heat recovery method according to claim 2, wherein a fourth circulation pump (27) for pumping the medium water in the water collector (26) is installed in a pipe at the front end of the collector, and the front end of the fourth circulation pump is connected to a water storage tank (39).
4. The float glass waste heat recovery method according to claim 1, wherein the intermediate water of 24 to 26 ℃ at the cold ends of the condensers of the first heat pump (23), the second heat pump (24), and the third heat pump (25) is supplied from a first water separator (28).
5. The float glass waste heat recovery method according to claim 1, wherein in the power-off state, the second control valve (4) is closed, the first control valve (3) is opened, and water in the preliminary water tank (2) is able to provide cooling water for the float glass plant (1) for 15 minutes.
6. The float glass waste heat recovery method according to claim 1, wherein the hot tank (22) and the cold tank (21) are separated by a heat insulation layer (20), and an overflow port (19) for communicating the two tanks is arranged on the heat insulation layer (20), so that water in the hot tank (22) or the cold tank (21) is excessive and exceeds the overflow port (19) to enter the corresponding tank, and the water is not directly overflowed from the tank due to excessive water storage in the separate tank.
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