CN115264986A - Low-temperature heat source driven second-class absorption heat pump device - Google Patents
Low-temperature heat source driven second-class absorption heat pump device Download PDFInfo
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- CN115264986A CN115264986A CN202111238516.6A CN202111238516A CN115264986A CN 115264986 A CN115264986 A CN 115264986A CN 202111238516 A CN202111238516 A CN 202111238516A CN 115264986 A CN115264986 A CN 115264986A
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- 238000010521 absorption reaction Methods 0.000 title claims abstract description 67
- 239000006096 absorbing agent Substances 0.000 claims abstract description 136
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 102
- AMXOYNBUYSYVKV-UHFFFAOYSA-M lithium bromide Chemical compound [Li+].[Br-] AMXOYNBUYSYVKV-UHFFFAOYSA-M 0.000 claims abstract description 22
- 239000000498 cooling water Substances 0.000 claims description 20
- 239000002918 waste heat Substances 0.000 abstract description 17
- 238000004519 manufacturing process Methods 0.000 abstract description 12
- 230000008929 regeneration Effects 0.000 abstract description 2
- 238000011069 regeneration method Methods 0.000 abstract description 2
- 239000003507 refrigerant Substances 0.000 description 55
- 239000007788 liquid Substances 0.000 description 48
- 238000000034 method Methods 0.000 description 13
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 8
- 238000010438 heat treatment Methods 0.000 description 8
- 229910000831 Steel Inorganic materials 0.000 description 6
- 229920006395 saturated elastomer Polymers 0.000 description 6
- 239000010959 steel Substances 0.000 description 6
- 239000000126 substance Substances 0.000 description 6
- 238000005265 energy consumption Methods 0.000 description 5
- 238000009835 boiling Methods 0.000 description 4
- 230000007423 decrease Effects 0.000 description 4
- 229910052742 iron Inorganic materials 0.000 description 4
- 238000010586 diagram Methods 0.000 description 3
- 239000002440 industrial waste Substances 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- 230000002745 absorbent Effects 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 230000002265 prevention Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000011946 reduction process Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
Images
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
- 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
- F25B37/00—Absorbers; Adsorbers
-
- 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
- F25B39/00—Evaporators; Condensers
- F25B39/02—Evaporators
-
- 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
- F25B39/00—Evaporators; Condensers
- F25B39/04—Condensers
-
- 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
- F25B41/00—Fluid-circulation arrangements
- F25B41/40—Fluid line arrangements
-
- 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
- F25B2339/00—Details of evaporators; Details of condensers
- F25B2339/02—Details of evaporators
-
- 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
- F25B2339/00—Details of evaporators; Details of condensers
- F25B2339/04—Details of condensers
-
- 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
-
- 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
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Materials Engineering (AREA)
- Sorption Type Refrigeration Machines (AREA)
Abstract
The invention discloses a second-class absorption heat pump device driven by a low-temperature heat source, which comprises an absorber group and a generator group; the device divides a plurality of pressure areas and concentration areas along the length direction of the device; the device also comprises an evaporator group and a condenser group; the absorber group is internally provided with a first solution heat exchanger, and the generator group is provided with a second solution heat exchanger. The device of the invention utilizes the discarded industrial low-temperature waste heat to drive the lithium bromide to evaporate and absorb heat, and the device forms a low-power consumption manufacturing system capable of realizing the production of medium-high temperature hot water, thereby substantially realizing the equipment and special industrial equipment coefficient of the regeneration energy of the industrial low-temperature waste heat.
Description
Technical Field
The invention relates to the technical field of waste heat recovery, in particular to a second-class absorption heat pump device driven by a low-temperature heat source.
Background
In the prior art, a second type absorption heat pump utilizes waste heat discharged by chemical plants, iron and steel plants, power plants and the like, and a waste heat source with the temperature of about 70 ℃ produces hot water with the temperature of about 90 ℃ so as to provide heating for various buildings, residential quarters and the like or provide process hot water for industrial production.
However, waste heat with a low temperature of 35 ℃ to 65 ℃ cannot find a device and a way for efficient utilization, and is directly discharged through a cooling tower or a chimney. Therefore, the waste heat of about 30 ℃ wasted in factories is used as the heat source of the second absorption heat pump, the temperature is raised to more than 20 ℃, hot water of about 60 ℃ is produced to be used as domestic hot water, heating heat or process hot water, the cost of primary energy consumption is greatly saved, and the multiple effects of reducing emission and reducing heat cost are achieved for environmental pollution prevention and control and consumers.
In the prior art, the second type absorption heat pump uses waste heat at about 70 ℃ as a heat source to generate hot water at about 90 ℃ at the use side, so as to provide heating heat or hot water in a production process for various buildings, offices, markets, residential quarters and the like.
Referring to fig. 1, an evaporator 20 and an absorber 13 are provided on the high pressure side, and a solution heat exchanger in which a concentrated solution and a dilute solution, which have undergone heat exchange in the condenser 40 and the generator 30, and the absorber 13 and the generator 30, exchange heat with each other, is provided on the low pressure side. Waste heat generated in a power plant, a chemical plant, an iron and steel plant, etc. enters the generator 30, flows into the solution heat exchanger 52 from the absorber, exchanges heat with the dilute solution whose temperature has been reduced after exchanging heat with the concentrated solution, generates refrigerant vapor, and then, the temperature is reduced, and the refrigerant vapor flows into the evaporator 20. The generated refrigerant vapor flows into the condenser 40. The heat source water B1 flowing into the evaporator 20 exchanges heat with the refrigerant liquid in the evaporator 20 to generate refrigerant vapor, and the refrigerant vapor flows out and is discarded, and the generated refrigerant vapor flows into the absorber 13. The condenser 40 has the cooling water D1 flowing therein to condense the refrigerant vapor flowing from the generator 30, and the cooling water D1 rises in temperature and then flows out.
The absorber 13 has a lower temperature use side hot water A1 for heating or hot water inflow and outflow from the generator 30, exchanging heat with the dilute solution in the solution heat exchanger 52, to exchange heat with the increased temperature concentrated solution. The rich solution absorbs the refrigerant vapor flowing in from the evaporator 20, decreases in concentration, absorbs the refrigerant vapor, releases the absorption heat into the use-side hot water A1, increases the outlet temperature of the use-side hot water A1, and uses the use-side hot water A1 for domestic hot water, heating, or process heat.
The flow rate of the absorption liquid, generator 30 → solution heat exchanger 52 → absorber 13 → solution heat exchanger 52 → generator 30;
heat source water flow B1 generator 30 → evaporator 20;
cooling water flow D1 to condenser 40;
the side hot water A1 flows to the absorber 13.
In combination with the above prior art processes, there is a need for those skilled in the art to develop a second type absorption heat pump device that can utilize waste heat of about 30 ℃ discarded by factories as a heat source of a second type absorption heat pump, increase the temperature to above 20 ℃, and produce hot water of about 60 ℃ as domestic hot water, heating heat or process hot water.
Disclosure of Invention
The invention provides a low-temperature heat source driving second-class absorption heat pump device which enables high-energy-consumption enterprises such as power plants, chemical plants and iron and steel plants to generate and discard low-temperature waste heat in the production process, enables lithium bromide to form water to be fully gasified to generate phase change and absorb heat under the condition of sufficient temperature difference in the device, realizes multi-stage heat exchange in a small temperature difference and convection mode according to gradient pressure and concentration change, avoids condensation display in the evaporation process of the device in the prior art as far as possible in the system operation, enables the heat release performance of the lithium bromide and the heat conversion performance of the system to be remarkably improved, enables the temperature of a side water inlet to be greatly increased at an outlet, enables industrial waste heat to be regenerated and utilized, and enables industrial enterprises to obtain life and production process heat for process links or users at low cost in the energy conservation and emission reduction process.
In order to achieve the above purpose, the invention provides the following technical scheme:
the invention relates to a low-temperature heat source driving second-class absorption heat pump device, which comprises:
an absorber set integrated within the device; and
a generator set integrated within the device;
the device divides a plurality of pressure areas and concentration areas along the length direction of the device;
the device also includes:
an evaporator group connected to the absorber group; and
a condenser bank connected to the generator bank;
the absorber group is internally provided with a first solution heat exchanger, and the generator group is provided with a second solution heat exchanger.
Further, the device is divided into four gradient pressure areas along the length direction of the device;
the absorber group is divided into a first absorber, a second absorber, a third absorber and a fourth absorber according to four gradient pressure areas;
the absorber group is configured according to the working conditions at 40wt% LiBr-52wt% LiBr concentration:
the first absorber is a high-pressure absorber, the second absorber is a medium-high pressure absorber, the third absorber is a medium-low pressure absorber, and the fourth absorber is a low-pressure absorber;
the evaporator group and the absorber group are matched and configured into four evaporators which are respectively a first evaporator, a second evaporator, a third evaporator and a fourth evaporator;
the first evaporator is a high-pressure evaporator, the second evaporator is a medium-high pressure evaporator, the third evaporator is a medium-low pressure evaporator, and the fourth evaporator is a low-pressure evaporator;
the absorber group and the evaporator group form a first box body;
the first solution heat exchanger is integrated in the first box body.
Further, 40wt% LiBr to 52wt% LiBr concentration divided into four gradient concentration regions under the same pressure condition;
the generator group is divided into a first generator, a second generator, a third generator and a fourth generator according to concentration areas of four gradients;
the first generator is a high-concentration generator, the second generator is a medium-high concentration generator, the third generator is a medium-low concentration generator, and the fourth generator is a low-concentration generator;
the condenser group comprises a first condenser, a second condenser, a third condenser and a fourth condenser;
the generator is combined with the condenser group to form a second box body;
the second solution heat exchanger is integrated in the second box body.
Further, the heat source water is divided into two branches, namely generator heat source water communicated with the generator group and evaporator heat source water communicated with the evaporator group;
the first tank introduces hot water at the use side;
the second box body introduces cooling water;
the flow direction of the generator heat source water is opposite to the flow direction of the cooling water;
the flow direction of the evaporator heat source water is opposite to the flow direction of the use side hot water.
In the technical scheme, the second-class absorption heat pump device driven by the low-temperature heat source provided by the invention has the following beneficial effects:
the absorption heat pump of the invention works to separate the evaporator and the absorber into four pressure gradients respectively, so that the pressure of the evaporator, the concentration of the absorption liquid of the absorber and the absorption liquid are in uninterrupted connection with each other at different temperatures, the concentration of the absorption liquid is differentiated at each pressure section difference, the heat of the heat source water is extracted more fully, and the heat source water can be lower according to the requirements of the production process.
The condenser and the generator are configured to exchange heat even if the inlet temperature is low by performing heat source water on the side of the generator at the same pressure, and the first solution heat exchanger and the second solution heat exchanger are arranged on the lower part to form solution temperature flow sequence heat exchange, so that the heat exchange temperature of the concentrated solution is increased, and the performance of the concentrated solution is improved.
Drawings
In order to more clearly illustrate the embodiments of the present application or technical solutions in the prior art, the drawings needed to be used in the embodiments will be briefly described below, and it is obvious that the drawings in the following description are only some embodiments described in the present invention, and other drawings can be obtained by those skilled in the art according to the drawings.
Fig. 1 is a schematic diagram of a second type absorption heat pump unit system in the prior art;
fig. 2 is a configured durin diagram of a second-type absorption heat pump apparatus driven by a low-temperature heat source according to an embodiment of the present invention;
fig. 3 is a schematic diagram of a system for driving a second-type absorption heat pump device by a low-temperature heat source according to an embodiment of the present invention.
Description of reference numerals:
10. a first absorber; 11. a second absorber; 12. a third absorber; 13. a fourth absorber;
20. a fourth evaporator; 21. a third evaporator; 22. a second evaporator; 23. a first evaporator;
30. a first generator; 31. a second generator; 32. a third generator; 33. a fourth generator;
40. a first condenser; 41. a second condenser; 42. a third condenser; 43. a fourth condenser;
50. a first solution heat exchanger; 51. a second solution heat exchanger;
a1, using side hot water;
b1, heat source water;
b10, generator heat source water; b11, evaporator heat source water;
d1, cooling water.
Detailed Description
In order to make the technical solutions of the present invention better understood, those skilled in the art will now describe the present invention in further detail with reference to the accompanying drawings.
See fig. 2-3;
the invention relates to a low-temperature heat source driving second-class absorption heat pump device, which comprises:
an absorber set integrated within the device; and
a generator set integrated within the device;
the device divides a plurality of pressure areas and concentration areas along the length direction of the device;
the device also includes:
an evaporator group connected with the absorber group; and
a condenser group connected with the generator group;
the absorber set is provided with a first solution heat exchanger 50 and the generator set is provided with a second solution heat exchanger 51.
Preferably, the device of the present embodiment is divided into four gradient pressure regions along its length direction;
the absorber group is divided into a first absorber 10, a second absorber 11, a third absorber 12 and a fourth absorber 13 according to the pressure areas of four gradients;
the absorber group is configured according to the working conditions at 40wt% libr-52wt% libr concentration:
the first absorber 10 is a high-pressure absorber, the second absorber 11 is a medium-high pressure absorber, the third absorber 12 is a medium-low pressure absorber, and the fourth absorber 13 is a low-pressure absorber;
the evaporator group and the absorber group are configured into four evaporators in a matching manner, namely a first evaporator 23, a second evaporator 22, a third evaporator 21 and a fourth evaporator 20;
the first evaporator 23 is a high-pressure evaporator, the second evaporator 22 is a medium-high pressure evaporator, the third evaporator 21 is a medium-low pressure evaporator, and the fourth evaporator 20 is a low-pressure evaporator;
the absorber group and the evaporator group form a first box body;
a first solution heat exchanger 50 is integrated in the first tank.
40wt% LiBr to 52wt% LiBr concentration divided into four gradient concentration regions under the same pressure condition;
the generator group is divided into a first generator 30, a second generator 31, a third generator 32 and a fourth generator 33 according to the concentration regions of the four gradients;
the first generator 30 is a high concentration generator, the second generator 31 is a medium-high concentration generator, the third generator 32 is a medium-low concentration generator, and the fourth generator 33 is a low concentration generator;
the condenser group comprises a first condenser 40, a second condenser 41, a third condenser 42 and a fourth condenser 43;
the generator and the condenser are combined to form a second box body;
a second solution heat exchanger 51 is integrated in the second tank.
The structure of the device system comprises an absorber group (divided into a first absorber 10, a second absorber 11, a third absorber 12 and a fourth absorber 13), an evaporator group (divided into a first evaporator 23, a second evaporator 22, a third evaporator 21 and a fourth evaporator 20), a generator group (divided into a first generator 30, a second generator 31, a third generator 32 and a fourth generator 33), and a condenser group (divided into a first condenser 40, a second condenser 41, a third condenser 42 and a fourth condenser 43), wherein under the condition of not separating the condensers, a pressure area and a concentration area are divided in the length direction of the device on one device, the saturation temperature of the absorption liquid is increased along with the increase of the pressure of the evaporator group, and the temperature difference between the heat source water B1 and the use side hot water A1 is larger by combining the flowing direction of the concentration and the temperature of the absorption liquid and the flowing direction of the heat source water B1 and the use side hot water A1 and the cooling water D1 into a complete flow-direction heat exchange mechanism, so that the temperature difference between the heat source water B1 and the use side hot water A1 is smaller, and the temperature difference between the circulating pump is smaller; the method is characterized in that when the using side hot water A1 is used to produce outlet temperature at higher high temperature, an externally attached solution heat exchanger is cancelled, a first solution heat exchanger 50 and a second solution heat exchanger 51 are respectively arranged at the lower parts of an absorber group and a generator group in the device to match the concentration and temperature flow of absorption liquid, so that continuous small-temperature-difference multistage heat exchange is realized without temperature gaps, the performance of the device is improved by improving the heat exchange efficiency of the first solution heat exchanger 50 and the second solution heat exchanger 51, the temperature-rising outlet water temperature higher than the temperature of using side inlet water is provided, and the flow of heat source water B1, the using side hot water A1 and cooling water D1 is regulated and controlled in a smaller range.
The second-class absorption heat pump driven by the low-temperature heat source realizes effective evaporation and heat absorption of lithium bromide in a low-temperature (35 ℃) state, meets the cold and hot requirements of production process water in a maximum temperature difference mode, returns water or discharges water in a lower temperature mode, and realizes ultralow-temperature discharge of waste heat and cold and hot remanufacturing without obvious new energy consumption.
The heat source water B1 is divided into two branches, namely generator heat source water B10 communicated with the generator group and evaporator heat source water B11 communicated with the evaporator group;
the first tank introduces the use side hot water A1;
cooling water D1 is introduced into the second box body;
the flow direction of the generator heat source water B10 is opposite to the flow direction of the cooling water D1;
the flow direction of the evaporator heat source water B11 is opposite to the flow direction of the use-side hot water A1.
Among them, more specifically:
the fourth generator 33 exchanges heat with the dilute solution flowing from the second solution heat exchanger 51 into the second solution heat exchanger 51 in the third generator 32, and the generator heat source water B10 having a decreased temperature flows in and exchanges heat with the dilute solution to heat the dilute solution, thereby generating superheated refrigerant vapor having a temperature higher than the temperature of the absorption liquid corresponding to the saturation pressure. At this time, the dilute solution flows into the first condenser 40 at a pressure higher than the saturation temperature. On the other hand, the generated refrigerant vapor flows into the first condenser 40, and is condensed by the cooling water D1 to generate refrigerant vapor, and the generator heat source water B10 having a lowered temperature is discarded or recovered at a process temperature in a chemical plant, a steel plant, a power plant, or the like.
The third generator 32 exchanges heat with the generator heat source water B10, which has been reduced in temperature and exchanges heat with the dilute solution flowing from the fourth generator 33 in the second generator 31, and heats the dilute solution, thereby generating superheated refrigerant vapor having a temperature higher than the absorption liquid temperature corresponding to the saturation pressure. At this time, the dilute solution flows into the second condenser 41 at a saturation temperature corresponding to the pressure of the second condenser. On the other hand, the generated refrigerant vapor flows into the second condenser 41, is condensed by the cooling water D1, generates refrigerant vapor, and flows out of the fourth generator 33 as the generator heat source water B10 having a lowered temperature.
The second generator 31 exchanges heat with the medium-concentration solution flowing in from the third generator 32 in the first generator 30, and the generator heat source water B10 whose temperature is lowered flows in and exchanges heat, so that the medium-concentration solution is heated, thereby generating superheated refrigerant vapor having a temperature higher than the absorption liquid temperature corresponding to the saturation pressure. At this time, the medium-concentration solution flows in at a saturation temperature corresponding to the pressure of the third condenser 42. On the other hand, the generated refrigerant vapor flows into the third condenser 42, is condensed by the cooling water D1, and the generator heat source water B10, which generates the refrigerant vapor and lowers the temperature, flows out of the third generator 32.
The first generator 30 is fed with the concentrated solution flowing from the second generator 31 and the generator heat source water B10 using waste heat, and heats the concentrated solution by heat exchange to generate superheated refrigerant vapor having a temperature higher than the temperature of the absorbent solution corresponding to the saturation pressure. At this time, the inflowing concentrated solution enters a saturation temperature corresponding to the pressure of the fourth condenser 43. On the other hand, the generated refrigerant vapor flows into the fourth condenser 43, is condensed in the cooling water D1, and the generator heat source water B10, which generates the refrigerant vapor and has a reduced temperature, flows out of the second generator 31.
The condenser condenses the superheated refrigerant vapor generated by the fourth generator 33, the third generator 32, the second generator 31, and the first generator 30 by the cooling water D1. The condensed refrigerant liquid flows out to the first evaporator 23, the second evaporator 22, the third evaporator 21, and the fourth evaporator 20, respectively. The cooling water D1 flows in from the first condenser 40 in which the superheated refrigerant vapor has a low temperature, and flows out in the order of a high temperature.
The first evaporator 23 exchanges heat between the refrigerant liquid flowing from the fourth condenser 43 and the evaporator heat source water B11 using waste heat, heats the refrigerant liquid in a saturated temperature state, and generates refrigerant vapor. On the other hand, the generated refrigerant vapor is absorbed in the first absorber 10 by the rich solution flowing in from the first solution heat exchanger 50. The evaporator heat source water B11, which generates the refrigerant vapor and has a reduced temperature, flows out to the second evaporator 22.
The second evaporator 22 exchanges heat between the refrigerant liquid flowing from the third condenser 42 and the evaporator heat source water B11 flowing from the first evaporator 23, heats the refrigerant liquid in a saturated temperature state, and generates refrigerant vapor. On the other hand, the generated refrigerant vapor is absorbed in the second absorber 11 by the heavy rich solution flowing in from the first absorber 10. The evaporator heat source water B11, which generates the refrigerant vapor and has a reduced temperature, flows out to the third evaporator 21.
The third evaporator 21 exchanges heat between the refrigerant liquid flowing from the second condenser 41 and the evaporator heat source water B11 flowing from the second evaporator 22, heats the refrigerant liquid in a saturated temperature state, and generates refrigerant vapor. On the other hand, the generated refrigerant vapor is absorbed in the third absorber 12 by the middle lean solution flowing in from the second absorber 11. The evaporator heat source water B11, which generates the refrigerant vapor and has a reduced temperature, flows out to the fourth evaporator 20.
The fourth evaporator 20 exchanges heat between the refrigerant liquid flowing from the first condenser 40 and the evaporator heat source water B11 flowing from the third evaporator 21, heats the refrigerant liquid in a saturated temperature state, and generates refrigerant vapor. On the other hand, the generated refrigerant vapor is absorbed in the fourth absorber 13 by the lean solution flowing in from the third absorber 12. The evaporator heat source water B11, which produces refrigerant vapor with a reduced temperature, is either discarded or returned as required by the chemical, steel or power plant industries.
The first absorber 10 is fed in the first solution heat exchanger 50 by the supercooled rich solution which has undergone heat exchange in the first absorber 10 and has accumulated in the lower part of the first absorber 10 at a temperature lower than the rich solution temperature corresponding to the saturation pressure of the lean solution. The inflowing concentrated solution absorbs refrigerant vapor having a saturation pressure generated in the first evaporator 23, so that the concentration of the absorption liquid decreases, and the temperature of the absorption liquid increases as the boiling point increases. On the other hand, the hot water A1 on the use side flows through the heat exchanger of the first absorber 10, the heat of the increased temperature of the absorption liquid is absorbed into the hot water A1 on the use side, the temperature is increased, the absorption liquid subjected to the heating continuously absorbs the refrigerant vapor to the lower part of the first solution heat exchanger 50, the concentration is continuously reduced, the temperature of the absorption liquid is continuously increased, and the dilute solution after the absorption is finished and the concentration is reduced exchanges heat with the concentrated solution from the lower part of the first absorber 10 and then flows out to the second absorber 11. The hot water A1 at the use side exchanges heat with the absorption liquid in the heat exchanger of the first absorber 10, and flows out of the use side after the temperature is raised for use in life or heat production.
After the second absorber 11 completes heat exchange in the first absorber 10 and collects the medium-concentration solution in the lower portion of the first absorber 10 to exchange heat with the rich solution flowing in from the first solution heat exchanger 50, the medium-concentration solution in the lower portion of the first absorber 10 flows in. At this time, the medium-concentrated solution is an overheated medium-concentrated solution higher than the medium-concentrated solution saturation temperature corresponding to the saturation pressure of the second evaporator 22, and COP increases. The medium-concentration solution flowing in absorbs the refrigerant vapor of the saturated pressure generated by the second evaporator 22, so that the concentration of the absorption liquid is reduced, and the temperature of the absorption liquid is increased as the boiling point is increased. On the other hand, the inside of the heat exchanger of the second absorber 11 is flowed with the use side hot water A1, the heat of the rising absorption liquid temperature is sucked into the use side hot water A1, the temperature is raised, the absorption liquid which is robbed of heat continues to absorb the refrigerant vapor to the first lower part of the heat exchanger 11, the concentration continues to decrease, and the absorption liquid temperature continues to rise. The middle dilute solution with the absorption ending and the concentration reduced exchanges heat with the strong solution from the lower part of the second absorber 11 and then flows out to the third absorber 12. The used side hot water A1 exchanges heat with the absorption liquid in the first absorber 10 heat exchanger, and flows out of the first absorber 10 side after the temperature is raised.
The third absorber 12 allows the middle-dilute solution in the lower part of the second absorber 11 to flow in after the second absorber 11 completes heat exchange and the middle-dilute solution collected in the lower part of the second absorber 11 and the rich solution flowing in from the first solution heat exchanger 50 perform heat exchange. At this time, the middle-lean solution is a superheated heavy-concentrated solution having a saturation temperature higher than the middle-lean solution saturation temperature corresponding to the saturation pressure of the third evaporator 21, and COP increases. The inflowing diluted solution absorbs refrigerant vapor of saturated pressure generated by the third evaporator 21, so that the concentration of the absorption liquid is reduced, and the temperature of the absorption liquid is increased along with the increase of the boiling point. On the other hand, the hot water A1 on the use side flows through the heat exchanger of the third absorber 12, the heat of the rising absorption liquid temperature is absorbed into the hot water A1 on the use side, the temperature rises, the absorption liquid which is robbed of heat continues to absorb the refrigerant vapor to the lower part of the first solution heat exchanger 50, the concentration is continuously reduced, and the temperature of the absorption liquid is continuously increased. The weak solution whose concentration is reduced after the absorption is finished flows out to the fourth absorber 13 after exchanging heat with the strong solution from the lower part of the third absorber 12. The used side hot water A1 exchanges heat with the absorption liquid in the third absorber 12 heat exchanger, and flows out of the second absorber 11 side after the temperature is raised.
The fourth absorber 13 is configured such that the dilute solution at the lower portion of the third absorber 12 flows in after the third absorber 12 completes heat exchange and the dilute solution collected at the lower portion of the third absorber 12 exchanges heat with the rich solution flowing in from the first solution heat exchanger 50. At this time, the dilute solution is an overheated dilute solution having a dilute solution saturation temperature higher than the saturation pressure of the fourth evaporator 20, and COP increases. The dilute solution flowing in absorbs the refrigerant vapor having a saturation pressure generated in the fourth evaporator 20, so that the concentration of the absorption liquid decreases, and the temperature of the absorption liquid increases as the boiling point increases. On the other hand, the hot water A1 on the use side flows through the heat exchanger of the fourth absorber 13, the heat of the raised absorption liquid temperature is sucked into the hot water A1 on the use side, the temperature is raised, the absorption liquid which is subjected to the heating continuously absorbs the refrigerant vapor to the lower part of the first solution heat exchanger 50, the concentration is continuously reduced, and the temperature of the absorption liquid is continuously raised. The weak solution whose concentration has been reduced after the completion of the absorption is heat-exchanged with the strong solution from the lower portion of the fourth absorber 13, and then flows out to the second solution heat exchanger 51. On the other hand, the use-side hot water A1 heated in the use-side heat supply site and reduced in temperature exchanges heat with the absorption liquid in the fourth absorber 13 heat exchanger, increases in temperature, and flows out of the third absorber 12 side.
The first solution heat exchanger 50 includes that the rich solution flowing out from the first generator 30 exchanges heat in the first absorber 10, the second absorber 11, the third absorber 12, and the fourth absorber 13, exchanges heat with the dilute solution falling from the lower portion in order of lower temperature, and flows into the first absorber 10.
The second solution heat exchanger 51 comprises a first generator 30, a second generator 31, a third generator 32 and a fourth generator 33, wherein the dilute solution flowing out of the fourth absorber 13 exchanges heat with the concentrated solution descending at the lower part in the order of high temperature and flows into the fourth generator 33.
Using the flow sequence of the calorimetric water A1:
Flow sequence of generator heat source water B10:
Flow sequence of evaporator heat source water B11:
Flow sequence of cooling water D1:
Refrigerant flow sequence:
generator set → condenser set → evaporator set → absorber set → generator set.
Flow sequence of the absorption liquid:
the fourth generator 33 → the third generator 32 → the second generator 31 → the first generator 30 → the first solution heat exchanger 50 → the first absorber 10 → the second absorber 11 → the third absorber 12 → the fourth absorber 13 → the second solution heat exchanger 51 → the fourth generator 33.
In the device of the embodiment, the power consumption of the heat source water B1, the use side hot water A1, the cooling water D1 and the solution circulating pump is only equivalent to one twentieth to one twenty-fifth of the output power, the cop value is up to more than 20, the process waste heat can be extracted to the maximum extent in the running process of the unit, the ultralow-temperature discharge of the industrial waste heat is realized, and the requirement on the process return water temperature is directly met.
In the technical scheme, the second-class absorption heat pump device driven by the low-temperature heat source provided by the invention has the following beneficial effects:
the device of the invention utilizes the discarded industrial low-temperature waste heat to drive the lithium bromide to evaporate and absorb heat, and the device forms a low-power consumption manufacturing system capable of realizing the production of medium-high temperature hot water, and substantially realizes the equipment of the regeneration energy of the industrial low-temperature waste heat and the coefficient of special industrial equipment. The device is arranged in large quantity, industrial waste heat of power stations, iron and steel plants, chemical plants and various high-energy-consumption enterprises is fully recovered and utilized, primary energy consumption can be saved in a large scale in the whole society, a few billions of tons of carbon dioxide are reduced, and the comprehensive production cost can be further reduced on the basis of optimizing the process structure and level of industrial finished products.
The absorption heat pump of the invention works to separate the evaporator and the absorber into four pressure gradients respectively, so that the pressure of the evaporator, the concentration of the absorption liquid of the absorber and the absorption liquid are in uninterrupted connection with each other at different temperatures, the concentration of the absorption liquid is differentiated at each pressure section difference, the heat of the heat source water is extracted more fully, and the heat source water can be lower according to the requirements of the production process.
The condenser and the generator are configured to exchange heat even if the inlet temperature is low by performing heat source water on the generator side at the same pressure, and the first solution heat exchanger and the second solution heat exchanger are arranged at the lower part to form solution temperature flow sequence heat exchange, so that the heat exchange temperature of the concentrated solution is increased, and the performance of the concentrated solution is improved.
While certain exemplary embodiments of the present invention have been described above by way of illustration only, it will be apparent to those of ordinary skill in the art that the described embodiments may be modified in various different ways without departing from the spirit and scope of the invention. Accordingly, the drawings and description are illustrative in nature and should not be construed as limiting the scope of the invention.
Claims (3)
1. The second kind absorption heat pump device driven by low temperature heat source is characterized in that the device includes:
an absorber set integrated within the device; and
a generator set integrated within the device;
the device divides a plurality of pressure areas and concentration areas along the length direction of the device;
the device also includes:
an evaporator group connected to the absorber group; and
a condenser bank connected to the generator bank;
a first solution heat exchanger (50) is arranged in the absorber group, and a second solution heat exchanger (51) is arranged in the generator group;
the heat source water (B1) is divided into two branches, namely generator heat source water (B10) communicated with the generator group and evaporator heat source water (B11) communicated with the evaporator group;
the first tank introduces use-side hot water (A1);
the second tank introduces cooling water (D1);
the flow direction of the generator heat source water (B10) is opposite to the flow direction of the cooling water (D1);
the flow direction of the evaporator heat source water (B11) is opposite to the flow direction of the use-side hot water (A1).
2. A low temperature heat source driven second-type absorption heat pump apparatus according to claim 1, wherein the apparatus is divided along its length into four gradient pressure zones;
the absorber group is divided into a first absorber (10), a second absorber (11), a third absorber (12) and a fourth absorber (13) according to four gradient pressure areas;
the absorber group is configured according to the working conditions at 40wt% LiBr-52wt% LiBr concentration:
the first absorber (10) is a high-pressure absorber, the second absorber (11) is a medium-high pressure absorber, the third absorber (12) is a medium-low pressure absorber, and the fourth absorber (13) is a low-pressure absorber;
the evaporator group and the absorber group are matched and configured into four evaporators, namely a first evaporator (23), a second evaporator (22), a third evaporator (21) and a fourth evaporator (20);
the first evaporator (23) is a high-pressure evaporator, the second evaporator (22) is a medium-high pressure evaporator, the third evaporator (21) is a medium-low pressure evaporator, and the fourth evaporator (20) is a low-pressure evaporator;
the absorber group and the evaporator group form a first box body;
the first solution heat exchanger (50) is integrated into the first tank.
3. A low temperature heat source driven second-type absorption heat pump apparatus according to claim 2, wherein under the same pressure conditions, 40wt% libr-52wt% libr concentration is divided into four gradient concentration regions;
the generator group is divided into a first generator (30), a second generator (31), a third generator (32) and a fourth generator (33) according to concentration regions of four gradients;
the first generator (30) is a high concentration generator, the second generator (31) is a medium-high concentration generator, the third generator (32) is a medium-low concentration generator, and the fourth generator (33) is a low concentration generator;
the condenser group comprises a first condenser (40), a second condenser (41), a third condenser (42) and a fourth condenser (43);
the generator is combined with the condenser group to form a second box body;
the second solution heat exchanger (51) is integrated in the second tank.
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| JP2007248013A (en) * | 2006-03-17 | 2007-09-27 | Ebara Corp | Absorption heat pump device, and its operating method |
| CN101650095A (en) * | 2009-09-03 | 2010-02-17 | 清华大学 | Multistage absorption refrigerating/heat pump unit |
| CN109269150A (en) * | 2017-07-17 | 2019-01-25 | 荏原冷热系统株式会社 | Absorption heat pump |
| CN215983309U (en) * | 2021-10-25 | 2022-03-08 | 河北安丰智域新能源装备制造有限公司 | Low-temperature heat source driven second-class absorption heat pump device |
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2021
- 2021-10-25 CN CN202111238516.6A patent/CN115264986B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2007248013A (en) * | 2006-03-17 | 2007-09-27 | Ebara Corp | Absorption heat pump device, and its operating method |
| CN101650095A (en) * | 2009-09-03 | 2010-02-17 | 清华大学 | Multistage absorption refrigerating/heat pump unit |
| CN109269150A (en) * | 2017-07-17 | 2019-01-25 | 荏原冷热系统株式会社 | Absorption heat pump |
| CN215983309U (en) * | 2021-10-25 | 2022-03-08 | 河北安丰智域新能源装备制造有限公司 | Low-temperature heat source driven second-class absorption heat pump device |
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