CN111351106A - Method for post-heating and supplying float glass by heat pump output heat exchange water - Google Patents
Method for post-heating and supplying float glass by heat pump output heat exchange water Download PDFInfo
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- CN111351106A CN111351106A CN201811565135.7A CN201811565135A CN111351106A CN 111351106 A CN111351106 A CN 111351106A CN 201811565135 A CN201811565135 A CN 201811565135A CN 111351106 A CN111351106 A CN 111351106A
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 472
- 238000010438 heat treatment Methods 0.000 title claims abstract description 56
- 239000005329 float glass Substances 0.000 title claims abstract description 55
- 238000000034 method Methods 0.000 title claims abstract description 27
- 239000002918 waste heat Substances 0.000 claims abstract description 43
- 238000001816 cooling Methods 0.000 claims abstract description 36
- 238000011084 recovery Methods 0.000 claims abstract description 27
- 239000000498 cooling water Substances 0.000 claims abstract description 10
- 238000004519 manufacturing process Methods 0.000 claims abstract description 10
- 230000008569 process Effects 0.000 claims abstract description 4
- AMXOYNBUYSYVKV-UHFFFAOYSA-M lithium bromide Chemical compound [Li+].[Br-] AMXOYNBUYSYVKV-UHFFFAOYSA-M 0.000 claims description 168
- 238000003860 storage Methods 0.000 claims description 49
- 238000005338 heat storage Methods 0.000 claims description 16
- 230000008859 change Effects 0.000 claims description 13
- 239000007789 gas Substances 0.000 claims description 9
- 238000005086 pumping Methods 0.000 claims description 7
- 238000004064 recycling Methods 0.000 claims description 2
- 238000009826 distribution Methods 0.000 abstract description 5
- 230000000694 effects Effects 0.000 abstract description 3
- 238000012546 transfer Methods 0.000 description 9
- 239000000446 fuel Substances 0.000 description 6
- 230000008878 coupling Effects 0.000 description 5
- 238000010168 coupling process Methods 0.000 description 5
- 238000005859 coupling reaction Methods 0.000 description 5
- 238000009413 insulation Methods 0.000 description 5
- 239000002699 waste material Substances 0.000 description 5
- 230000008901 benefit Effects 0.000 description 4
- 238000010248 power generation Methods 0.000 description 4
- 238000009434 installation Methods 0.000 description 3
- 230000005855 radiation Effects 0.000 description 3
- 230000033228 biological regulation Effects 0.000 description 2
- 238000004891 communication Methods 0.000 description 2
- 125000004122 cyclic group Chemical group 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000004134 energy conservation Methods 0.000 description 2
- 239000002440 industrial waste Substances 0.000 description 2
- 239000012774 insulation material Substances 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
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- 238000004146 energy storage Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 230000020169 heat generation Effects 0.000 description 1
- 230000008092 positive effect Effects 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 238000009423 ventilation Methods 0.000 description 1
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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
- F24D3/00—Hot-water central heating systems
- F24D3/18—Hot-water central heating systems using heat pumps
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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
- F24D3/00—Hot-water central heating systems
- F24D3/10—Feed-line arrangements, e.g. providing for heat-accumulator tanks, expansion tanks ; Hydraulic components of a central heating system
-
- 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
- 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
- F25B27/00—Machines, plants or systems, using particular sources of energy
- F25B27/02—Machines, plants or systems, using particular sources of energy using waste heat, e.g. from internal-combustion engines
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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
- F24D2200/00—Heat sources or energy sources
- F24D2200/32—Heat sources or energy sources involving multiple heat sources in combination or as alternative heat sources
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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
- F24D2220/00—Components of central heating installations excluding heat sources
- F24D2220/10—Heat storage materials, e.g. phase change materials or static water enclosed in a space
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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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A30/00—Adapting or protecting infrastructure or their operation
- Y02A30/27—Relating to heating, ventilation or air conditioning [HVAC] technologies
- Y02A30/274—Relating to heating, ventilation or air conditioning [HVAC] technologies using waste energy, e.g. from internal combustion engine
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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 method for post-heating and supplying float glass by heat pump output heat exchange water belongs to the field of heat supply waste heat recovery and heat distribution, and aims to solve the problems that a low-temperature heat source and a high-temperature heat source are mixed for heat exchange, the heating requirement can be met in heating, the use of the high-temperature heat source is reduced, the self-circulation of intermediate water is realized, and the heat is reasonably distributed, wherein circulating water at the temperature of 37-39 ℃ in a heat pool is extracted by a circulating pump of a water feeding pipe and is directly extracted to a cooling tower 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, the temperature of the cooling water in the process flow production is required to be 20-30 ℃, the outlet of the low-temperature heat exchange section is connected with the first inlet of the water mixer and conveys low-temperature heat exchange water (38-42 ℃) to the water mixer, the outlet of the water collector is communicated with the second inlet of the water mixer and conveys recovered water (33-35 ℃) to the water mixer, the low-temperature heat exchange water and the recovered water are mixed in the water mixer to form mixed water, and the effect is that high-temperature heat and low-temperature heat are output together.
Description
Technical Field
The invention belongs to the field of heat supply waste heat recovery and heat distribution, and relates to a method for post-heating and supplying float glass by heat pump output heat exchange water.
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 problems that a low-temperature heat source and a high-temperature heat source are mixed for heat exchange, the heating requirement can be met in heating, the use of the high-temperature heat source is reduced, the self-circulation of intermediate water is realized, and the heat is reasonably distributed, the invention provides the following technical scheme:
a method for post-heating and supplying float glass by heat pump output heat exchange water comprises a float glass waste heat recovery method and a lithium bromide heat pump heating method;
the method for recycling the waste heat of the float glass comprises the steps of introducing circulating water at 37-39 ℃ generated in a float glass workshop into a hot pool through a first water pipe, pressurizing a second circulating pump and a third circulating pump, opening an eighth control valve, a ninth control valve, a tenth control valve and an eleventh control valve after pressurization, closing the third control valve, the fourth control valve, the fifth control valve and the sixth control valve, opening a seventh control valve, pumping the circulating water at 37-39 ℃ in the hot pool through the circulating pump of a water feeding pipe, pumping the circulating water to evaporators in a first heat pump, a second heat pump and a third heat pump, inputting the circulating water at 37-39 ℃ and intermediate water at 24-26 ℃ at a cold end of a condenser, outputting the intermediate water at 33-35 ℃ at the hot end of the condenser after heat exchange, outputting the circulating water at 31-33 ℃ at a cold end of the evaporator, supplying the circulating water to a cooling tower, cooling the circulating water by the cooling tower and discharging the circulating water into a cold pool, 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. 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, 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 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 and then discharged into the cold pool, 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.
The hot ends of the condensers of the first heat pump, the second heat pump and the third heat pump output medium water with the temperature of 33-35 ℃ and are collected by a water collector. A pipeline at the front end of the water collector is provided with a fourth circulating pump for pumping intermediate water in the water collector, and the front end of the fourth circulating pump is communicated with a second inlet of a water mixer of the lithium bromide heat pump heating device;
according to the heating method of the lithium bromide heat pump, a condenser lead-in pipe of a power plant is communicated with a high-temperature heat exchange section of the lithium bromide heat pump, high-temperature heat exchange water (100 ℃) is conveyed to the high-temperature heat exchange section, an outlet of the high-temperature heat exchange section is communicated with an inlet of a low-temperature heat exchange section, the heat exchange water (60 ℃) after high-temperature heat exchange is conveyed to the low-temperature heat exchange section, an outlet of the low-temperature heat exchange section is connected with a first inlet of a water mixer and conveys low-temperature heat exchange water (38-42 ℃) to the water mixer, an outlet of a water collector is communicated with a second inlet of the water mixer and conveys recycled water (33-35 ℃) to the water mixer, the low-temperature heat exchange water and the recycled water are mixed in the water mixer to form mixed water (36-38 ℃), an outlet of the water mixer is connected with a hot end of an evaporator of a fourth heat pump and conveys mixed water (36-38 ℃) to the hot end), the mixed water, and the condensed gas return pipe of the power plant is used for conveying the water back to the power plant, the rest water (8-12 ℃) is conveyed to the water storage tank to be used as return water, the temperature of the return water is detected by the temperature sensor, if the detected temperature is lower than a set threshold (24 ℃), the solar water heater is started to heat the return water or the phase change heat storage device releases stored heat to heat the return water in the water storage tank, the temperature of the return water is increased, and the return water can be stabilized at the set threshold (24-26 ℃).
Has the advantages that: the condensate water of the power plant is expensive, the float glass water is low in use price, the cost of only using the water of the power plant as the high-temperature heat source of the lithium bromide heat pump is too high, the intermediate water of the float glass waste heat is obtained as the low-temperature heat source, the use amount of the water of the power plant is greatly reduced, the economic benefit is improved, a large amount of low-temperature heat sources can be provided to be coupled with the high-temperature steam provided by the power plant for heat supply, under the condition that the heat supply effect is not influenced, the use amount of the high-temperature steam of the power plant is greatly reduced, the low-temperature heat source generated by the float glass plant is. Has positive effect on realizing the target of energy conservation and emission reduction. Lithium bromide heat pump heating system is to the storage water, carried out the heat transfer between user side and the power plant water, supply the user side with the heat of high temperature power plant water and storage water, through the lithium bromide heat pump promptly, the heat transfer is accomplished to the heat pump, 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, water source and thermal saving and make full use of have been realized.
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 preparation 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. the system comprises a temperature sensor, 30, a fifteenth control valve, 31, a water storage tank, 32, a fifth circulating pump, 33, a phase change heat storage device, 34, a thirteenth control valve, 35, a fourteenth control valve, 36, a solar water heater, 37, a sixteenth control valve, 38, a lithium bromide heat pump, 39, a user end pipeline, 40, a fourth heat pump, 41, a cogeneration device, 42, a water mixer, 43, a water dividing valve, 44, a second water divider, 45, a power plant condensed gas return pipe and 46, and a sixth circulating pump.
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 other outlet of a water dividing valve of the lithium bromide heat pump heating device is connected with the inlet of a water storage tank of the solar waste heat recovery device, the outlet of the water storage tank (31) of the solar waste heat recovery device is communicated with a first water divider (28), and the cold end input of the condenser of the heat pump (23, 24, 25) is the first water divider (28).
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). A fourth circulating pump (27) for pumping intermediate water in the water collector (26) is installed on a pipeline at the front end of the water collector, the other outlet of the water dividing valve of the lithium bromide heat pump heating device is connected with an inlet of a water storage tank of the solar waste heat recovery device, an outlet of the water storage tank (31) of the solar waste heat recovery device is communicated with the first water divider (28), and the cold end input of the condenser of the heat pump (23, 24, 25) is the first water divider (28).
The intermediate water with the temperature 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 divider (28), the water supply of the first water divider (28) comes from a water storage tank of a solar waste heat recovery device, the water supply of the water storage tank comes from a lithium bromide heat pump heating device, the returned water after heat exchange is used as the intermediate water with the temperature of 24-26 ℃ to form the intermediate water for float glass waste heat recovery, the intermediate water is subjected to heat exchange by the lithium bromide heat pump heating device to form high heat source supply, the low-temperature water after heat exchange is reheated by the solar waste heat recovery device and reaches a water source suitable for float glass reuse, namely the lithium bromide heat pump heating device performs heat exchange on the part of heat and high-temperature hot water of a power plant to a user pipeline, the float glass waste heat and the solar waste heat are used as heating sources, and the intermediate water after heat exchange is used for outputting from the cold end of, the circulation 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 (33), a water storage tank (31), a temperature sensor (29), a fifth circulating pump (32), a thirteenth control valve (34), a fourteenth control valve (35) and a fifteenth control valve (30), wherein a circulating outlet of the water storage tank (31) is connected with the solar water heater (36) through a pipeline, a fifteenth control valve (30) is arranged on the pipeline section, a water outlet pipe of the solar water heater (36) is branched into two paths which are connected with water pipes in parallel, a thirteenth control valve (34) is arranged on one water pipe, and is connected with the fifth circulating pump (32), a fourteenth control valve (35) is arranged on the other water pipe, and is connected with a phase change heat storage device (33), the phase change heat storage device (33) is connected with the fifth circulating pump (32), and the outlet of the fifth circulating pump (32) is connected with the circulating inlet of the water storage tank (31). The inlet of the water storage tank (31) is connected with one outlet of a water dividing valve of the lithium bromide heat pump heating device, the outlet of the water storage tank is connected with a first water divider of the float glass waste heat recovery device, and the first water divider is connected with more than one heat pump (23, 24, 25) and connected with the cold end of a condenser of the heat pump (23, 24, 25).
The execution method of the device comprises the following steps: the solar energy waste heat recovery method comprises the following steps:
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 (30), closing a fourteenth control valve (35), opening a thirteenth control valve (34), so that water in the water storage tank (31) is extracted by a fifth circulating pump (32) from a circulating outlet of the water storage tank (31), the water in the water storage tank (31) is heated by a solar water heater (36), the heated water is directly extracted to the water storage tank (31) through a pipeline provided with the thirteenth control valve (34), and the heated water flows back to the water storage tank (31) from a circulating water inlet of the water storage tank (31); 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 (31) 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 (30), closing a thirteenth control valve (34), opening a fourteenth control valve (35), starting a phase change heat storage device (33), enabling water in a water storage tank (31) to be extracted by a fifth circulating pump (32) from a circulating outlet of the water storage tank (31), heating the water in the water storage tank (31) by a solar water heater (36), and enabling the phase change heat storage device (33) to store excessive heat energy through a pipeline provided with the phase change heat storage device (33), so that the outlet water temperature is kept 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 (34), opening the fourteenth control valve (35), starting the phase-change heat storage device (33), so that water in the water storage tank (31) is pumped out by the fifth circulating pump (32) from a circulating outlet of the water storage tank (31), the water in the water storage tank (31) is heated by the solar water heater (36), and heat energy stored in a heat storage mode is released by the phase-change heat storage device (33) through a pipeline provided with the phase-change heat storage device (33), 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 of operation, the first and second modes,
the inlet of the water storage tank (31) is connected with one outlet of a water dividing valve of the lithium bromide heat pump heating device, the outlet of the water storage tank is connected with a first water divider of the float glass waste heat recovery device, and the first water divider is connected with more than one heat pump (23, 24, 25) and connected with the cold end of a condenser of the heat pump (23, 24, 25).
The lithium bromide heat pump heating device comprises a lithium bromide heat pump (38), a fourth heat pump (40), a water mixer (42), a water separator (44) and a water storage tank (31); the lithium bromide heat pump (38) comprises a high-temperature heat exchange section, a low-temperature heat exchange section and a medium-temperature heat exchange section, the water mixer (42) comprises a first inlet, a second inlet and an outlet, and a condenser of the fourth heat pump (40) is connected with a second output pipeline; the inlet of the high-temperature heat exchange section is connected with a heat and power cogeneration device (41), the outlet of the high-temperature heat exchange section is connected with the inlet of the low-temperature heat exchange section, the outlet of the low-temperature heat exchange section is connected with the first inlet of a water mixer (42), the outlet of a water collector (26) is communicated with the second inlet of the water mixer (42), the outlet of the water mixer (42) is connected with the hot end of an evaporator of a fourth heat pump (40), the cold end of the evaporator is connected with a second water separator (44), a two-way water distribution valve (43) is installed on the second water separator (44), one outlet of the water distribution valve (43) is connected with a condensate gas return pipe (45) of a power plant, the other outlet of the water distribution valve (43) is connected with the inlet of a water storage tank (31) of a solar waste heat recovery device, a fifteenth control valve (30) is installed on a connected pipeline, and the solar waste, A water storage tank (31), a temperature sensor (29), a fifth circulating pump (32), a thirteenth control valve (34), a fourteenth control valve (35) and a sixteenth control valve (37), wherein the temperature sensor (29) is installed in the water storage tank (31), an outlet of the water storage tank (31) is connected with the solar water heater through a pipeline, the sixteenth control valve (37) is arranged on the pipeline section, a water outlet pipe of the solar water heater is branched into two parallel water pipes, the thirteenth control valve (34) is arranged on one water pipe and connected with the fifth circulating pump (32), the fourteenth control valve (35) is arranged on the other water pipe and connected with a phase change heat storage device (33), the fifth circulating pump (32) is connected with the phase change heat storage device (33), an outlet of the fifth circulating pump (32) is connected with a circulating inlet of the water storage tank (31), a medium-temperature heat exchange section of the lithium bromide heat pump (38) is connected with a first output pipeline, the condenser end of the fourth heat pump (40) is connected with the second output pipeline.
And a sixth circulating pump (46) is arranged in a connecting pipeline between the outlet of the shunt valve (43) and the inlet of the water storage tank (31). And a fourth circulating pump (27) is arranged on a communication pipeline between the outlet of the water collector (26) and the second inlet of the water mixer (42). The outlet of the water storage tank (31) is connected with a first water divider (28), the first water divider (28) is connected with more than one heat pump (23, 24, 25) and is connected with the cold end of the condenser of the heat pump (23, 24, 25). The first output pipeline and the second output pipeline are connected with the user side pipeline and output heat exchange heat energy in a grading mode. The user side pipeline is a heat supply pipeline. The cogeneration device (41) is connected to a power plant, wherein the steam temperature is about 100 ℃, the input temperature of a high-temperature heat exchange section of the lithium bromide heat pump (38) is about 100 ℃, the output temperature is about 60 ℃, the input temperature of a low-temperature heat exchange section is about 60 ℃, the output temperature is about 38-42 ℃, the input temperature of a medium-temperature heat exchange section is about 45 ℃, and the output temperature is about 60 ℃; the output temperature of mixed water of the water mixer (42) is 36-38 ℃, the input temperature of hot end input of the evaporator of the fourth heat pump (40) is 36-38 ℃, the output temperature of the cold end is 8-12 ℃, the input temperature of the cold end of the condenser is about 36 ℃, the output temperature of the hot end is about 45 ℃, and the temperature of water output from the water storage tank (31) is about 24-26 ℃.
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 execution method of the device comprises the following steps: a lithium bromide heat pump heating method includes that a condenser lead-in pipe of a power plant is communicated with a high-temperature heat exchange section of a lithium bromide heat pump (38), high-temperature heat exchange water (100 ℃) is conveyed to the high-temperature heat exchange section, an outlet of the high-temperature heat exchange section is communicated with an inlet of a low-temperature heat exchange section, the heat exchange water (60 ℃) after high-temperature heat exchange is conveyed to the low-temperature heat exchange section, an outlet of the low-temperature heat exchange section is connected with a first inlet of a water mixer (42) and conveys low-temperature heat exchange water (38-42 ℃) to the water mixer (42), an outlet of a water collector (26) is communicated with a second inlet of the water mixer (42) and conveys recycled water (33-35 ℃) to the water mixer (42), the low-temperature heat exchange water and the recycled water are mixed in the water mixer (42) to form mixed water (36-38 ℃), an outlet of the water mixer (42) is connected with a hot end of an evaporator of a fourth heat pump, after heat exchange, water is separated by a second water separator (44), the second water separator (44) separates water (8-12 ℃) which is equal to the water input by the cogeneration device (41), the water is conveyed to the power plant by a power plant condensed gas return pipe (45), the rest water (8-12 ℃) is conveyed to a water storage tank (31) to be used as return water, a temperature sensor (29) detects the temperature of the return water, if the detected temperature is lower than a set threshold (24 ℃), a solar water heater is started to heat the return water or a phase change heat storage device (33) releases stored heat to heat the return water in the water storage tank (31), and the temperature of the return water is increased and can be stabilized at the set threshold (24-26 ℃). Arrange lithium bromide heat pump heating system behind the solar energy waste heat recovery device in, its purpose on the one hand rearmounted heating can obtain the water supply of lithium bromide demand temperature, and does not arrange lithium bromide heat pump heating system in front of it, is in order to obtain lower power plant condensation return water.
The middle-temperature heat exchange section of the lithium bromide heat pump (38) is connected with a first output pipeline (with the input temperature of 45 degrees), the high-temperature heat exchange section and the low-temperature heat exchange section exchange heat with the middle-temperature heat exchange section (with the output temperature of 60 degrees), the evaporator section of the fourth heat pump (40) exchanges heat with the condenser section (with the output temperature of 45 degrees and the input temperature of 36 degrees), and the heat exchange heat energy is output in a grading manner. The return water, the temperature of which is stabilized at the set threshold value, is delivered to a first water separator (28) to be reused. The client is a user heating pipeline. And return water (24-26 ℃) 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 high-temperature heat exchange water is 100 ℃, the low-temperature heat exchange water is 38-42 ℃, the medium-temperature water output by the medium-temperature heat exchange section is 60 ℃, and the backwater is 25 ℃; the heat exchange water after heat exchange in the high-temperature heat exchange section is 60 ℃, the condensed water is 5 ℃, and the output low-temperature water at the hot end of the condenser is 36 ℃. The method comprises the following steps that the power plant is in limited production or overhaul operation to cause the yield of condensed water to be reduced, the water inflow of high-temperature heat exchange water from a condensed gas water conduit 41 of the power plant is reduced, the power of a lithium bromide heat pump (38) is adjusted and reduced, the water outlet temperature of the lithium bromide heat pump (38) is maintained to be 38-42 ℃, the water is mixed with water of 34-36 ℃ output by a float glass waste heat recovery device, the temperature of the mixed water reaches 36-38 ℃, the mixed water enters a heat pump 40, the heat exchange is water of 8-12 ℃, the mixed water enters a second water separator (44), water which is equal to the inflow water of a condensed water inlet pipe of the power plant is separated by the second water separator (44) and is conveyed back to the power plant, and the residual water separated by the water separator is conveyed to a; when a float glass plant is overhauled, the yield of cooling water of the float glass plant is reduced, the power of a lithium bromide heat pump (38) is adjusted and improved, the outlet water temperature of the lithium bromide heat pump (38) is maintained to be 38-42 ℃, the outlet water is mixed with water of 34-36 ℃ output by a float glass waste heat recovery device, the mixed water temperature reaches 36-38 ℃, the mixed water enters a fourth heat pump (40), the heat exchange is water of 8-12 ℃, the mixed water enters a second water separator (44), water which is equal to the inlet water of a condensate water inlet pipe of a power plant is separated by the water separator and is conveyed back to the power plant, and the residual water separated by the water separator is conveyed to a water storage tank (31).
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 hot water supply and the intermediate water of the power plant are clean, and the device only uses the low-temperature waste heat carried by the hot water supply and the intermediate water, so the hot water supply and the intermediate water can be used in a mixed way, and the use amount of high-temperature water of the power plant is greatly reduced because a large amount of low-temperature waste heat which is not used in a float glass workshop is utilized, and because the cold pool water in the float glass workshop is low in price, the load and the operation cost of the power plant are reduced, and the heating area is increased.
The system designs a redundant heating mode that multiple energy sources are mutually backup, and can still heat the tail end of a user when the heat which can be provided by a power plant or a float glass plant for some reason is reduced; for example, when the power plant is limited by environmental protection factors or maintenance, the yield of condensed water is reduced, or the yield of low-temperature waste heat is reduced due to the limitation of yield or maintenance factors of float glass, the whole coupling heating system can still provide stable heating load, the operation reliability of the heating system is improved, and the stability of central heating of northern towns, which is an important civil engineering, is ensured. Specifically, in a power plant or a float glass plant where production is limited, the following control modes are designed:
when the power plant is in limited production or overhaul operation, the yield of condensed water is reduced, the water inflow from a condensed gas water conduit 41 of the power plant is reduced at the moment, the power of a lithium bromide heat pump is reduced, the water outlet temperature of the lithium bromide heat pump 38 is improved through internal regulation of the lithium bromide heat pump system, the water with the water outlet temperature of 38-42 ℃ of the lithium bromide heat pump 38 is mixed with the water temperature of 34-36 ℃ recovered by float glass waste heat and then reaches 36-38 ℃, then the mixed water enters a fourth heat pump 40, the heat exchange is water with the temperature of 8-12 ℃, the mixed water enters a second water separator 44, the water with the same amount as the water inflow from a condensed water inlet 41 of the power plant is separated out and.
When the float glass factory overhauls, the cooling water yield of float glass factory reduces, improve the power of lithium bromide heat pump, through the inside regulation of lithium bromide heat pump system, the leaving water temperature of lithium bromide heat pump 38, the lithium bromide heat pump 38 goes out the water and reaches 27 ~ 28 ℃ after the water by float glass waste heat recovery 34 ~ 36 ℃ mixes, then gets into fourth heat pump 40, the heat transfer is 8 ~ 12 ℃ of water, get into second water separator 44, divide this moment and the power plant condensate water inlet 41 equal amount's water return power plant, another part is sent into water storage tank 31.
The outlet water temperature of the lithium bromide heat pump is reduced, the temperature difference is enlarged, the cooling water of the power plant is more effectively utilized, the utilization rate of low-temperature waste heat is improved, and the lithium bromide heat pump water charging system is more suitable for charging the water of the power plant according to the flow rate instead of the heat quantity and needs related matched devices of the power plant. The solar device is arranged between the second water divider 44 and the first water divider 28 instead of between the water collector 26 and the water mixer 42, and the solar device is specially used for supplying heat to the return water, so that the temperature of the return water is stable, and the stability of the system is improved.
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.
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 (1)
1. A method for post-heating and supplying float glass by heat pump output heat exchange water is characterized by comprising a float glass waste heat recovery method and a lithium bromide heat pump heating method;
the method for recycling the waste heat of the float glass 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 the 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 condensers of the first heat pump (23), the second heat pump (24) and the third heat pump (25) output 33-35 ℃ intermediate water to be collected by a water collector (26), a pipeline at the front end of the water collector is provided with a fourth circulating pump (27) for pumping the intermediate water in the water collector (26), and the front end of the fourth circulating pump (27) is communicated with a second inlet of a water mixer of the lithium bromide heat pump heating device;
the lithium bromide heat pump heating method comprises the steps that a condenser lead-in pipe of a power plant is communicated with a high-temperature heat exchange section of a lithium bromide heat pump (38) and conveys high-temperature heat exchange water to the high-temperature heat exchange section, an outlet of the high-temperature heat exchange section is communicated with an inlet of a low-temperature heat exchange section and conveys heat exchange water after high-temperature heat exchange to the low-temperature heat exchange section, an outlet of the low-temperature heat exchange section is connected with a first inlet of a water mixer (42) and conveys low-temperature heat exchange water to the water mixer (42), an outlet of a water collector (26) is communicated with a second inlet of the water mixer (42) and conveys recovered water to the water mixer (42), the low-temperature heat exchange water and the recovered water are mixed in the water mixer (42) to form mixed water, an outlet of the water mixer (42) is connected with a hot end of an evaporator of a fourth heat pump (40) and conveys mixed water to the water, the mixed water is subjected to heat exchange by the fourth heat pump (40), a second water separator (44, and the condensed gas is conveyed back to the power plant by a power plant condensed gas return pipe (45), the rest water is conveyed to a water storage tank (31) to be used as return water, the temperature of the return water is detected by a temperature sensor (29), if the detected temperature is lower than a set threshold value, a solar water heater is started to heat the return water or a phase change heat storage device (33) releases stored heat to heat the return water in the water storage tank (31), and the temperature of the return water is increased and can be stabilized at the set threshold value.
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