CN112268382A - Novel large-temperature-difference heat exchange unit adopting circulation mode - Google Patents
Novel large-temperature-difference heat exchange unit adopting circulation mode Download PDFInfo
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- CN112268382A CN112268382A CN202011292822.3A CN202011292822A CN112268382A CN 112268382 A CN112268382 A CN 112268382A CN 202011292822 A CN202011292822 A CN 202011292822A CN 112268382 A CN112268382 A CN 112268382A
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- 239000006096 absorbing agent Substances 0.000 claims abstract description 128
- 239000003507 refrigerant Substances 0.000 claims abstract description 111
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 82
- 238000005507 spraying Methods 0.000 claims abstract description 33
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 claims abstract description 21
- 238000003860 storage Methods 0.000 claims description 20
- 239000007788 liquid Substances 0.000 claims description 11
- 239000007921 spray Substances 0.000 claims description 9
- 238000000605 extraction Methods 0.000 claims description 7
- 239000000243 solution Substances 0.000 description 123
- AMXOYNBUYSYVKV-UHFFFAOYSA-M lithium bromide Chemical group [Li+].[Br-] AMXOYNBUYSYVKV-UHFFFAOYSA-M 0.000 description 31
- 238000010025 steaming Methods 0.000 description 14
- 238000004519 manufacturing process Methods 0.000 description 12
- 239000000463 material Substances 0.000 description 8
- 238000001514 detection method Methods 0.000 description 7
- 238000005192 partition Methods 0.000 description 6
- 238000010521 absorption reaction Methods 0.000 description 5
- 238000003466 welding Methods 0.000 description 5
- 238000005086 pumping Methods 0.000 description 4
- 238000001816 cooling Methods 0.000 description 3
- 238000000034 method Methods 0.000 description 3
- 238000005452 bending Methods 0.000 description 2
- 239000012141 concentrate Substances 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 230000003014 reinforcing effect Effects 0.000 description 2
- 230000002745 absorbent Effects 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 238000003892 spreading Methods 0.000 description 1
- 239000011550 stock solution Substances 0.000 description 1
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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
- F25B33/00—Boilers; Analysers; Rectifiers
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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
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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
- F25B39/00—Evaporators; Condensers
- F25B39/04—Condensers
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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
- F25B2500/00—Problems to be solved
- F25B2500/01—Geometry problems, e.g. for reducing size
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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
- F25B2500/00—Problems to be solved
- F25B2500/05—Cost reduction
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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
- F25B2500/00—Problems to be solved
- F25B2500/09—Improving heat transfers
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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
- F25B2500/00—Problems to be solved
- F25B2500/17—Size reduction
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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
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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
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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)
- Power Engineering (AREA)
- Sorption Type Refrigeration Machines (AREA)
Abstract
The invention discloses a novel circulation type large temperature difference heat exchange unit; comprises a generator, a condenser, an evaporator group, an absorber group and a water-plate heat exchanger; the generator is connected with the primary net water inlet, the water-water plate type heat exchanger, the evaporator group and the primary net water outlet in sequence; the water-water plate type heat exchanger is communicated with a secondary net water inlet and a secondary net water outlet through a secondary net water pipeline, and the secondary net water inlet is sequentially connected with the absorber group, the condenser and the secondary net water outlet through pipelines; the absorber group is connected with a first solution pipeline, the first solution pipeline is communicated with the generator after passing through the solution heat exchanger, the generator is communicated with a second solution pipeline, and the second solution pipeline is connected with the top of the absorber group after passing through the solution heat exchanger; the bottom of the condenser is communicated with a refrigerant pipeline communicated with the evaporator group, and the bottom of the evaporator group is connected with a refrigerant pump and an evaporator group spraying device through the refrigerant pipeline. The invention has simple structure, small heat exchange area and high heat exchange efficiency.
Description
Technical Field
The invention relates to the field of heat exchange equipment, in particular to a novel circulation type large-temperature-difference heat exchange unit.
Background
The lithium bromide unit is also called lithium bromide absorption heat pump unit or large temperature difference heat supply unit, and is a device for producing hot water for heating in vacuum state by using circulating water of heat supply network as heat source, water as refrigerant and lithium bromide water solution as absorbent.
Disclosure of Invention
The invention aims to provide a novel circulation type large-temperature-difference heat exchange unit, which solves the problems in the prior art and has the advantages of simple structure, small heat exchange area and high heat exchange efficiency.
In order to achieve the purpose, the invention provides the following scheme:
the invention provides a novel circulation type large-temperature-difference heat exchange unit which comprises a generator, a condenser, an evaporator group, an absorber group and a water-water plate type heat exchanger, wherein the absorber group comprises a low-pressure absorber and a high-pressure absorber, and the evaporator group comprises a low-pressure evaporator and a high-pressure evaporator; the generator and the condenser are arranged in first closed equipment, a steam circulation channel is arranged between the generator and the condenser, a solution outlet disc is arranged at the bottom of the generator, a refrigerant outlet disc is arranged at the bottom of the condenser, the low-pressure absorber and the low-pressure evaporator are arranged in second closed equipment, the high-pressure absorber and the high-pressure evaporator are arranged in third closed equipment, the second closed equipment is arranged above the third closed equipment, and the second closed equipment and the third closed equipment are communicated and share a set of air extraction system; a steam circulation channel is arranged between the low-pressure absorber and the low-pressure evaporator, and a steam circulation channel is arranged between the high-pressure absorber and the high-pressure evaporator; the high-pressure absorber and the low-pressure absorber only need one solution pump, the low-pressure absorber and the high-pressure absorber are only provided with one solution storage disc, the high-pressure evaporator and the low-pressure evaporator only need one refrigerant pump, and the low-pressure evaporator and the high-pressure evaporator are only provided with one refrigerant storage disc; one end of the generator is connected with a primary net water inlet, the other end of the generator is connected with a water-water plate type heat exchanger through a primary net water pipeline, the water-water plate type heat exchanger is communicated with the evaporator group through the primary net water pipeline, and the evaporator group is communicated with a primary net water outlet; the water-water plate type heat exchanger is respectively communicated with a secondary net water inlet and a secondary net water outlet through a secondary net water pipeline, and the secondary net water inlet is sequentially connected with the absorber group, the condenser and the secondary net water outlet in series through pipelines; a solution storage tray at the bottom of the low-pressure absorber is communicated with the high-pressure absorber through a pipeline, the solution storage tray at the bottom of the high-pressure absorber is connected with a first solution pipeline, a solution pump is arranged on the first solution pipeline, intermediate liquid formed after concentrated solution in the low-pressure absorber absorbs refrigerant steam of the low-pressure evaporator enters the high-pressure absorber for spraying, the intermediate liquid absorbs the refrigerant steam of the high-pressure evaporator, finally joins with solution in the solution storage tray of the high-pressure absorber and enters a solution heat exchanger through the solution pump, the first solution pipeline is communicated with a spraying device at the top of the generator after passing through the solution heat exchanger, the bottom of the generator is communicated with a second solution pipeline, and the second solution pipeline is connected with the spraying device at the top of the low-pressure absorber after passing through the solution heat exchanger; the refrigerant liquid outlet disc at the bottom of the condenser is communicated with a first refrigerant pipeline, the first refrigerant pipeline is communicated with a spraying device at the top of the high-pressure evaporator, the refrigerant at the bottom of the low-pressure evaporator is connected with a second refrigerant pipeline, the refrigerant at the bottom of the high-pressure evaporator is communicated with the second refrigerant pipeline through a pipeline and then is connected with a refrigerant pump, and the refrigerant pump is communicated with the spraying devices at the tops of the low-pressure evaporator and the high-pressure evaporator through a third refrigerant pipeline.
Optionally, the water-water plate heat exchanger is connected in series with the high-pressure evaporator and the low-pressure evaporator through a primary water network pipeline, and the low-pressure evaporator is communicated with a primary water network outlet; and the secondary net water inlet is communicated with the low-pressure absorber and the high-pressure absorber in parallel through pipelines and then is connected with the condenser and the secondary net water outlet in series.
Optionally, the bottom of the high-pressure absorber is connected with a first solution pipeline, the first solution pipeline is communicated with the spraying device at the top of the generator after passing through the solution heat exchanger, the bottom of the generator is communicated with a second solution pipeline, the second solution pipeline is connected with the spraying device at the top of the low-pressure absorber after passing through the solution heat exchanger, and the bottom of the low-pressure absorber is connected with the spraying device at the top of the high-pressure absorber through a third solution pipeline. The solution circulates in series through the generator, the low-pressure absorber and the high-pressure absorber adopt an up-and-down arrangement structure, only a solution storage disc needs to be arranged at the bottom, the structure is simple, the amount of the solution needing to be added to the unit is reduced, and the volume of the unit is reduced.
Optionally, the bottom of the low-pressure evaporator and the bottom of the high-pressure evaporator are respectively connected with the refrigerant pump through a second refrigerant pipeline, the refrigerant pump is respectively communicated with the spray devices at the tops of the low-pressure evaporator and the high-pressure evaporator through a third refrigerant pipeline, and the bottom of the condenser is communicated with the spray device at the top of the high-pressure evaporator through a branch between the first refrigerant pipeline and the third refrigerant pipeline and the high-pressure evaporator.
Optionally, the generator and the condenser are arranged in a first closed device, the low-pressure absorber and the low-pressure evaporator are arranged in a second closed device, the high-pressure absorber and the high-pressure evaporator are arranged in a third closed device, and the second closed device and the third closed device are communicated with each other and share one set of air extraction system.
Optionally, the low-pressure absorber and the high-pressure absorber are arranged in an up-down structure, and the low-pressure evaporator and the high-pressure evaporator are arranged in an up-down structure.
Optionally, the solution pump is disposed between the solution heat exchanger and the absorber group.
Compared with the prior art, the invention has the following technical effects:
under the same working condition and the same load requirement, the heat exchange area of the circulation mode of the invention is smaller than that of the traditional single-steaming single-absorbing circulation mode, thereby reducing the unit volume, the whole solution amount and the cost of the solution pump. Compared with the traditional double-steaming double-suction circulation mode, the upper cylinder is changed into a generator and a condenser by two generators and two condensers, the lower cylinder is provided with the absorber and the evaporator in a second closed device and a third closed device which are communicated, so that only one set of air pumping system is needed, and then only one time of detection is needed during detection of vacuum and the like, the detection man-hour is reduced, and the unit cost is reduced from multiple aspects for the traditional double-steaming double-suction circulation mode. Only need detect once, detect man-hour and reduce. The solution pump and the refrigerant pump are changed into one pump from two pumps, the cost of the pump is reduced, the total solution circulation amount is reduced by 55%, and the cost of the solution pump is further reduced. The total circulating amount of the lithium bromide solution can be reduced by 55% at most compared with the circulating amount of the total lithium bromide solution in a traditional double-steaming double-absorbing circulating mode, the amount of the lithium bromide solution required by a unit is reduced, and the unit cost is reduced; the electrical control system is changed from two sides to one side, the electrical control cost is reduced by about 30%, the electrical devices are reduced, and the material cost and the manufacturing time are reduced.
According to the invention, the low-pressure absorber and the low-pressure evaporator are arranged in one closed device, the high-pressure absorber and the high-pressure evaporator are arranged in one closed device, and the two closed devices are communicated up and down, so that the unit cost is reduced from multiple aspects, and the working hours of blanking, bending and other working procedures in the manufacturing process are greatly reduced. The upper barrel and the lower barrel of the original double-steaming double-suction circulation mode structure need an intermediate partition plate to be divided into two independent cavities, the welding requirement on the partition plate is high, and the leakage-proof detection is carried out on the welding of the partition plate. Solution piping and refrigerant piping such as a solution pump base and a refrigerant pump unit are changed from two-side piping to one-side piping, the number of the piping is reduced by 30%, the amount of lithium bromide solution and refrigerant is reduced, the material cost of the piping is reduced, the manufacturing cost of the piping is reduced, and the amount of the unit solution is reduced. Two sets of air extraction systems required by the closed equipment arranged on the evaporator and the absorber are changed into one set, so that the manufacturing working hour and the material cost are reduced. The high-low pressure absorber is changed into an upper structure and a lower structure from a left structure and a right structure, the water pan of the absorber is reduced by half, the lithium bromide solution required by the liquid storage pan of the unit absorber is reduced by about 40 percent, and the solution cost is reduced. The waterway piping and the water chamber piping avoid the cross piping which is difficult to operate, and the attractiveness, the manufacturing operability and the unit maintenance convenience of the waterway piping and the water chamber piping are enhanced.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the 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 of the present invention, and it is obvious for those skilled in the art to obtain other drawings without inventive exercise.
FIG. 1 is a schematic structural diagram of a novel circulation type large temperature difference heat exchange unit;
wherein, 1 is a generator, 2 is a condenser, 3 is a steam circulation channel, 4 is a primary network water inlet, 5 is a primary network water pipeline, 6 is a water-water plate type heat exchanger, 7 is a primary network water outlet, 8 is a secondary network water pipeline, 9 is a secondary network water inlet, 10 is a secondary network water outlet, 11 is a first solution pipeline, 12 is a solution heat exchanger, 13 is a second solution pipeline, 14 is a solution pump, 15 is a first refrigerant pipeline, 16 is a second refrigerant pipeline, 17 is a refrigerant pump, 18 is a third refrigerant pipeline, 19 is a low-pressure absorber, 20 is a high-pressure absorber, 21 is a low-pressure evaporator, 22 is a high-pressure evaporator, and 23 is a third solution pipeline.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
The invention aims to provide a novel circulation type large-temperature-difference heat exchange unit, which solves the problems in the prior art and has the advantages of simple structure, small heat exchange area and high heat exchange efficiency.
In order to make the aforementioned objects, features and advantages of the present invention comprehensible, embodiments accompanied with figures are described in further detail below.
The traditional large-temperature-difference heat exchange unit mainly comprises a single-steaming single-absorbing circulation mode structure and a double-steaming double-absorbing circulation mode structure at present; based on the defects of the traditional heat exchange structures, the invention provides a novel circulation type large-temperature-difference heat exchange unit which comprises a generator 1, a condenser 2, an evaporator group, an absorber group and a water-water plate type heat exchanger 6, wherein the generator 1 is connected with the condenser 2 through a pipeline; a steam circulation channel 3 is arranged between the generator 1 and the condenser 2, and a steam circulation channel 3 is arranged between the evaporator group and the absorber group; one end of the generator 1 is connected with a primary net water inlet 4, the other end of the generator is connected with a water-water plate type heat exchanger 6 through a primary net water pipeline 5, the water-water plate type heat exchanger 6 is communicated with an evaporator group through the primary net water pipeline 5, and the evaporator group is communicated with a primary net water outlet 7; the water-water plate type heat exchanger 6 is respectively communicated with a secondary net water inlet 9 and a secondary net water outlet 10 through a secondary net water pipeline 8, and the secondary net water inlet 9 is sequentially connected with the absorber group, the condenser 2 and the secondary net water outlet 10 in series through pipelines; the bottom of the absorber group is connected with a first solution pipeline 11, the first solution pipeline 11 is communicated with a spraying device at the top of the generator 1 after passing through a solution heat exchanger 12, the bottom of the generator 1 is communicated with a second solution pipeline 13, the second solution pipeline 13 is connected with the spraying device at the top of the absorber group after passing through the solution heat exchanger 12, the first solution pipeline 11 is provided with a solution pump 14, the solution pump 14 is arranged between the solution heat exchanger 12 and the absorber group, and the solution pipeline is used for conveying a lithium bromide solution; the bottom of the condenser 2 is communicated with a first refrigerant pipeline 15, the first refrigerant pipeline 15 is communicated with the evaporator group, the bottom of the evaporator group is connected with a refrigerant pump 17 through a second refrigerant pipeline 16, and the refrigerant pump 17 is communicated with a spraying device at the top of the evaporator group through a third refrigerant pipeline 18. The absorber group comprises a low pressure absorber 19 and a high pressure absorber 20, and the evaporator group comprises a low pressure evaporator 21 and a high pressure evaporator 22. The generator 1 and the condenser 2 are arranged in the first closed device, a steam circulation channel 3 is arranged between the generator 1 and the condenser 2, a solution outlet disc is arranged at the bottom of the generator 1, and a refrigerant outlet disc is arranged at the bottom of the condenser 2; the low-pressure absorber 19 and the low-pressure evaporator 21 are arranged in a second closed device, the high-pressure absorber 20 and the high-pressure evaporator 22 are arranged in a third closed device, the second closed device is arranged above the third closed device, namely the low-pressure absorber 19 is arranged above the high-pressure absorber 20, the low-pressure evaporator 21 is arranged above the high-pressure evaporator 22, and the second closed device and the third closed device share one set of air extraction system; a steam circulation channel 3 is arranged between the low-pressure absorber 19 and the low-pressure evaporator 21, and a steam circulation channel 3 is arranged between the high-pressure absorber 20 and the high-pressure evaporator 22; the bottom parts of the low-pressure absorber 19 and the high-pressure absorber 20 are only provided with one solution storage disc, and the bottom parts of the low-pressure evaporator 21 and the high-pressure evaporator 22 are only provided with one refrigerant storage disc. The solution storage tray at the bottom of the high-pressure absorber 20 is connected with a first solution pipeline 11, a solution pump 12 is arranged on the first solution pipeline 11, concentrated solution in the low-pressure absorber 19 absorbs refrigerant steam of the low-pressure evaporator and then becomes intermediate liquid to enter the high-pressure absorber 20 for spraying, meanwhile, solution after absorbing refrigerant steam of the high-pressure evaporator and solution in the solution storage tray of the high-pressure absorber 20 are converged and then enter the solution heat exchanger 12 through a solution pump 14, and the first solution pipeline 11 is communicated with a spraying device at the top of the generator 1 after passing through the solution heat exchanger 12. The first refrigerant pipeline 15 is communicated with a spraying device at the top of the high-pressure evaporator 22, the refrigerant at the bottom of the low-pressure evaporator 21 is connected with a second refrigerant pipeline 16, the refrigerant at the bottom of the high-pressure evaporator 22 is communicated and converged with the second refrigerant pipeline 16 through a pipeline and then is connected with a refrigerant pump 17, and the refrigerant pump 17 is respectively communicated with the spraying devices at the tops of the low-pressure evaporator 21 and the high-pressure evaporator 22 through a third refrigerant pipeline 18.
It is further preferred that the low pressure absorber 19 is disposed above the high pressure absorber 20, so that only one solution storage pan needs to be disposed at the bottom of the absorber bank; the low-pressure evaporator 21 is arranged above the high-pressure evaporator 22, so that only one refrigerant liquid storage disc is arranged at the bottom of the evaporator group. The water-water plate type heat exchanger 6 is connected with the high-pressure evaporator 22 and the low-pressure evaporator 21 in series through the primary net water pipeline 5, and the low-pressure evaporator 21 is communicated with a primary net water outlet 7; the secondary net water inlet 9 is communicated with the low-pressure absorber 19 and the high-pressure absorber 20 in parallel through pipelines and then is connected with the condenser 2 and the secondary net water outlet 10 in series. The bottom of the high-pressure absorber 20 is connected with a first solution pipeline 11, the first solution pipeline 11 is communicated with a spraying device at the top of the generator 1 after passing through a solution heat exchanger 12, the bottom of the generator 1 is communicated with a second solution pipeline 13, the second solution pipeline 13 is connected with the spraying device at the top of the low-pressure absorber 19 after passing through the solution heat exchanger 12, and the bottom of the low-pressure absorber 19 is connected with the spraying device at the top of the high-pressure absorber 20 through a third solution pipeline 23. The bottom of the low-pressure evaporator 21 and the bottom of the high-pressure evaporator 22 are respectively connected with a refrigerant pump 17 through a second refrigerant pipeline 16, the refrigerant pump 17 is respectively communicated with the spray devices at the tops of the low-pressure evaporator 21 and the high-pressure evaporator 22 through a third refrigerant pipeline 18, and the bottom of the condenser 2 is communicated with the spray device at the top of the high-pressure evaporator 22 after being converged by a branch from the third refrigerant pipeline 18 to the high-pressure evaporator 22 through a first refrigerant pipeline 15. The generator 1 and the condenser 2 are arranged in a first closed device, the low-pressure absorber 19 and the low-pressure evaporator 21 are arranged in a second closed device, the high-pressure absorber 20 and the high-pressure evaporator 22 are arranged in a third closed device, and the second closed device and the third closed device share one set of air extraction system. The absorber set and the evaporator set can be made into an integral water chamber structure, the structure is simpler, and cross piping which is difficult to operate is avoided.
The high-pressure side and the low-pressure side of the lithium bromide solution are in series connection, and the circulation mode during working is as follows:
lithium bromide solution side: dilute solution enters a solution heat exchanger from a high-pressure absorber through a solution pump to exchange heat with concentrated solution and then enters a generator, the generator concentrates the dilute solution into concentrated solution, the concentrated solution comes out from the generator to enter the solution heat exchanger to exchange heat with the dilute solution and then enters a low-pressure absorber to be sprayed, the concentrated solution absorbs refrigerant steam of a low-pressure evaporator to be diluted into intermediate solution, the intermediate solution enters the high-pressure absorber to absorb the refrigerant steam generated by the high-pressure evaporator to be diluted into dilute solution, the dilute solution continues to circulate, and monitoring and control of the vacuum degree of the whole circulation loop can be realized only by a set of measuring and measuring system.
Refrigerant side: the generator concentrates the dilute solution to generate refrigerant steam, the refrigerant steam enters the condenser, and the condenser generates refrigerant water. Refrigerant water in the condenser directly enters a spraying device of the high-pressure evaporator for spraying, does not enter a water tray of the evaporator for flashing any more, enters the spraying device of the high-pressure evaporator for spraying, and then reaches the spraying device of the evaporator group for spraying through a refrigerant pump, so that the circulation amount of a refrigerant circulating pump is reduced; the model of refrigerant pump reduces, and the low pressure evaporimeter sprays surplus refrigerant water and joins at the stock solution dish refrigerant export of high pressure evaporimeter through the second refrigerant pipeline, later divides the spray set that two the way got into low pressure evaporimeter and high pressure evaporimeter respectively through the refrigerant pump and sprays, has reduced a refrigerant pump, and the whole volume of equipment reduces.
Refrigerant water of a liquid storage disc of the high-pressure evaporator is divided into two paths by a refrigerant pump, one path of the refrigerant water is conveyed to the low-pressure evaporator to be sprayed and evaporated to generate refrigerant steam, the refrigerant steam is absorbed by concentrated solution of a low-pressure absorber through a steam circulation channel 3, the concentrated solution is changed into intermediate solution, the other path of the refrigerant water and the refrigerant water of the condenser are conveyed to enter a high-pressure generator spreading device to be sprayed and evaporated to generate refrigerant steam, the refrigerant steam is absorbed by the intermediate solution of the high-pressure absorber through the steam circulation channel 3, the intermediate solution is changed into dilute solution, and the dilute solution continues. The low-pressure evaporator and the low-pressure absorber are connected by a vapor flow channel 3, and the high-pressure evaporator and the high-pressure absorber are connected by another vapor flow channel 3.
An external waterway:
primary net watering: the primary net water is cooled through the generator for the first time, continuously enters the water-water plate type heat exchanger to carry out secondary cooling with the secondary net water, continuously enters the high-pressure evaporator to carry out tertiary cooling, continuously enters the low-pressure evaporator to carry out quaternary cooling, and then enters the demand area from the low-pressure evaporator.
And secondary net water, wherein the secondary net water is divided into two paths, one path enters the water-water plate type heat exchanger to exchange heat with the primary net water, the other path is divided into two paths to respectively reach the high-pressure absorber and the low-pressure absorber to be heated for the first time, then the two paths are combined and enter the condenser to be heated for the second time, and the secondary net water coming out of the water-water plate type heat exchanger and the secondary net water coming out of the condenser are combined into one path to enter the.
Compared with the traditional single-steaming single-absorbing circulation mode, the circulation mode of the invention is as follows:
under the same working condition and the same load, the heat exchange area of the circulation mode is small, and the heat exchange area can be reduced by 20% under some special working conditions.
Compared with the traditional double-steaming double-suction circulation mode, the circulation mode of the heat exchanger unit provided by the invention is as follows:
under the same working condition and the same load. The upper closed equipment (high-temperature cylinder) in the circulating mode is changed into one generator and one condenser from two generators and two condensers, and the lower closed equipment (low-temperature cylinder) is combined into one communicated equipment from two independent evaporation and absorption cylinder bodies, so that the structure reduces the unit cost from multiple aspects.
Specifically, the invention has the following advantages:
1. reduction of material cost
The lower cylinder of the closed equipment is changed from narrow to high, so that the width of the upper cylinder plate and the lower cylinder plate is reduced, the height of the side plates is increased, the stress area of the upper cylinder plate and the lower cylinder plate is reduced, the number of reinforcing ribs of the upper cylinder plate and the lower cylinder plate is reduced, and the working time for welding the reinforcing ribs is reduced. The side plates are corrugated plates which are thinner than the upper and lower cylinder plates but have high strength, so that the material cost is reduced.
The solution pump and the refrigerant pump are changed into one pump from two pumps, the cost of the pump is reduced, the total solution circulation amount and the refrigerant circulation amount are reduced by 55%, the models of the solution pump and the refrigerant pump can be selected to be small, and the cost is further reduced.
Compared with the traditional circulation modes of single-steaming single-absorption and double-steaming double-absorption, the total circulation quantity of the lithium bromide solution can be reduced by 55 percent at most, the quantity of the lithium bromide solution required by a unit is reduced, and the cost of the lithium bromide solution is reduced.
The solution tubing and the refrigerant tubing such as the solution pump base, the refrigerant pump set and the like are changed from two-side tubing to one-side tubing, the tubing is reduced by 30 percent, the tubing material cost is reduced, the lithium bromide solution and the refrigerant cost are reduced, and the tubing manufacturing cost is reduced
The high-pressure absorber and the low-pressure absorber are changed into an upper structure and a lower structure from a left structure and a right structure, the width of the absorber liquid storage disk is reduced by half, the lithium bromide solution required by the liquid storage disk of the unit absorber is reduced by about 40%, and the solution cost is reduced.
The second closed equipment where the low-pressure absorber and the low-pressure evaporator are located and the third closed equipment where the high-pressure absorber and the high-pressure evaporator are located adopt an up-and-down structure, so that the requirement of the whole unit on the vacuum environment can be met only by one set of air pumping system, the two sets of air pumping systems are changed into one set, the material cost is reduced, and the requirement on the vacuum environment is met
The electrical control system is changed from two sides to one side, the electrical control cost is reduced by about 30%, the electrical devices are reduced, and the material cost is reduced.
2. Reduction of manufacturing cost
The upper cylinder and the lower cylinder of the closed equipment are respectively combined into a cylinder by two independent cylinders, so that the processes of blanking, bending and the like in the manufacturing process are reduced.
The upper barrel and the lower barrel of the original double-steaming double-suction circulation mode structure respectively need the intermediate partition plate to be divided into two independent cavities, the welding requirement on the partition plate is high, the circulation mode of the invention reduces the intermediate partition plate, and reduces the welding requirement
The high-pressure water chamber and the low-pressure water chamber of the original double-steaming double-absorption circulating type structure unit are independently manufactured, the circulating type generator and the condenser are changed into one from two, the high-pressure absorber and the low-pressure absorber and the evaporator water chamber can be manufactured into an integral water chamber, and the number of the water chambers is reduced by half.
When the original double-steaming double-suction circulation type structure unit is used for vacuum detection and the like, the high pressure side and the low pressure side need to be detected firstly and then the other side needs to be detected, the detection working hours are more, the circulation mode of the invention can be only used for detecting once, and the detection working hours are reduced.
The solution piping and the refrigerant piping of the solution pump base, the refrigerant pump unit and the like are changed into one-side piping from two-side piping, the piping is reduced by 30 percent, and the manufacturing cost of the piping is reduced.
Two sets of air pumping systems are changed into one set, so that the manufacturing working hours are reduced.
The electric appliance control system is changed from two sides to one side, and the manufacturing working hours are reduced.
3. Appearance and others
The invention has more compact integral structure, especially occupies less space in the width direction, and has wider applicability to the field space of customers.
The electrical control system is changed from two sides to one side, so that control points are reduced, junction boxes and wiring pipelines are reduced, and the overall appearance of the unit is more concise.
The waterway piping and the water chamber piping avoid the cross piping which is difficult to operate, and the attractiveness, the manufacturing operability and the unit maintenance convenience of the waterway piping and the water chamber piping are enhanced.
The principle and the implementation mode of the invention are explained by applying a specific example, and the description of the embodiment is only used for helping to understand the method and the core idea of the invention; meanwhile, for a person skilled in the art, according to the idea of the present invention, the specific embodiments and the application range may be changed. In view of the above, the present disclosure should not be construed as limiting the invention.
Claims (7)
1. The utility model provides a big difference in temperature heat exchanger group of novel circulation mode which characterized in that: the system comprises a generator, a condenser, an evaporator group, an absorber group and a water-water plate type heat exchanger, wherein the absorber group comprises a low-pressure absorber and a high-pressure absorber, and the evaporator group comprises a low-pressure evaporator and a high-pressure evaporator; the generator and the condenser are arranged in first closed equipment, a steam circulation channel is arranged between the generator and the condenser, a solution outlet disc is arranged at the bottom of the generator, a refrigerant outlet disc is arranged at the bottom of the condenser, the low-pressure absorber and the low-pressure evaporator are arranged in second closed equipment, the high-pressure absorber and the high-pressure evaporator are arranged in third closed equipment, the second closed equipment is arranged above the third closed equipment, and the second closed equipment and the third closed equipment are communicated and share a set of air extraction system; a steam circulation channel is arranged between the low-pressure absorber and the low-pressure evaporator, and a steam circulation channel is arranged between the high-pressure absorber and the high-pressure evaporator; the high-pressure absorber and the low-pressure absorber only need one solution pump, the low-pressure absorber and the high-pressure absorber are only provided with one solution storage disc, the high-pressure evaporator and the low-pressure evaporator only need one refrigerant pump, and the low-pressure evaporator and the high-pressure evaporator are only provided with one refrigerant storage disc; one end of the generator is connected with a primary net water inlet, the other end of the generator is connected with a water-water plate type heat exchanger through a primary net water pipeline, the water-water plate type heat exchanger is communicated with the evaporator group through the primary net water pipeline, and the evaporator group is communicated with a primary net water outlet; the water-water plate type heat exchanger is respectively communicated with a secondary net water inlet and a secondary net water outlet through a secondary net water pipeline, and the secondary net water inlet is sequentially connected with the absorber group, the condenser and the secondary net water outlet in series through pipelines; the solution at the bottom of the low-pressure absorber is communicated with the high-pressure absorber through a pipeline, a solution storage tray at the bottom of the high-pressure absorber is connected with a first solution pipeline, a solution pump is arranged on the first solution pipeline, intermediate liquid formed after the concentrated solution in the low-pressure absorber absorbs refrigerant vapor of the low-pressure evaporator enters the high-pressure absorber for spraying, the refrigerant vapor of the high-pressure evaporator is absorbed and finally joins with the solution in the solution storage tray of the high-pressure absorber and then enters a solution heat exchanger through the solution pump, the first solution pipeline is communicated with a spraying device at the top of the generator after passing through the solution heat exchanger, the bottom of the generator is communicated with a second solution pipeline, and the second solution pipeline is connected with the spraying device at the top of the low-pressure absorber after passing through the solution; the refrigerant liquid outlet disc at the bottom of the condenser is communicated with a first refrigerant pipeline, the first refrigerant pipeline is communicated with a spraying device at the top of the high-pressure evaporator, the refrigerant at the bottom of the low-pressure evaporator is connected with a second refrigerant pipeline, the refrigerant at the bottom of the high-pressure evaporator is communicated with the second refrigerant pipeline through a pipeline and then is connected with a refrigerant pump, and the refrigerant pump is communicated with the spraying devices at the tops of the low-pressure evaporator and the high-pressure evaporator through a third refrigerant pipeline.
2. The novel large-temperature-difference heat exchange unit adopting the circulation mode as claimed in claim 1, characterized in that: the water-water plate type heat exchanger is connected with the high-pressure evaporator and the low-pressure evaporator in series through a primary net water pipeline, and the low-pressure evaporator is communicated with a primary net water outlet; and the secondary net water inlet is communicated with the low-pressure absorber and the high-pressure absorber in parallel through pipelines and then is connected with the condenser and the secondary net water outlet in series.
3. The novel large-temperature-difference heat exchange unit adopting the circulation mode as claimed in claim 1, characterized in that: the high-pressure absorber is characterized in that a first solution pipeline is connected to the bottom of the high-pressure absorber, the first solution pipeline is communicated with a spraying device at the top of the generator after passing through a solution heat exchanger, a second solution pipeline is communicated with the bottom of the generator and connected with the spraying device at the top of the low-pressure absorber after passing through the solution heat exchanger, and the bottom of the low-pressure absorber is connected with the spraying device at the top of the high-pressure absorber through a third solution pipeline.
4. The novel large-temperature-difference heat exchange unit adopting the circulation mode as claimed in claim 1, characterized in that: the low-pressure evaporator bottom and the high-pressure evaporator bottom are respectively connected with the refrigerant pump through second refrigerant pipelines, the refrigerant pump is respectively communicated with the spray devices at the tops of the low-pressure evaporator and the high-pressure evaporator through third refrigerant pipelines, and the condenser bottom is converged together from the third refrigerant pipeline to the high-pressure evaporator through a first refrigerant pipeline and is communicated with the spray device at the top of the high-pressure evaporator.
5. The novel large-temperature-difference heat exchange unit adopting the circulation mode as claimed in claim 1, characterized in that: the generator and the condenser are arranged in first closed equipment, the low-pressure absorber and the low-pressure evaporator are arranged in second closed equipment, the high-pressure absorber and the high-pressure evaporator are arranged in third closed equipment, and the second closed equipment and the third closed equipment are communicated and share one set of air extraction system.
6. The novel large-temperature-difference heat exchange unit adopting the circulation mode as claimed in claim 1, characterized in that: the low-pressure absorber and the high-pressure absorber are arranged in an up-and-down structure, and the low-pressure evaporator and the high-pressure evaporator are arranged in an up-and-down structure.
7. The novel large-temperature-difference heat exchange unit adopting the circulation mode as claimed in claim 1, characterized in that: the solution pump is disposed between the solution heat exchanger and the absorber group.
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| CN202011292822.3A CN112268382B (en) | 2020-11-18 | 2020-11-18 | Novel circulation mode large-temperature-difference heat exchanger unit |
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| CN112268382B CN112268382B (en) | 2024-04-30 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2022168460A1 (en) * | 2021-02-08 | 2022-08-11 | パナソニックＩｐマネジメント株式会社 | Evaporator unit for absorption refrigerator, heat exchange unit, and absorption refrigerator |
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| CN200986345Y (en) * | 2006-09-11 | 2007-12-05 | 东南大学 | Hot-water type lithium bromide absorbing refrigerator between single effect and two stage |
| CN109163474A (en) * | 2018-10-16 | 2019-01-08 | 山东金佰瑞节能科技有限公司 | One pump multistage absorption-multistage evaporation absorption heat pump processed and the method for increasing the temperature difference |
| CN111174464A (en) * | 2020-01-06 | 2020-05-19 | 同方节能装备有限公司 | Double-effect double-energy water chilling unit |
| CN213657168U (en) * | 2020-11-18 | 2021-07-09 | 同方节能装备有限公司 | Novel large-temperature-difference heat exchange unit adopting circulation mode |
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- 2020-11-18 CN CN202011292822.3A patent/CN112268382B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN200986345Y (en) * | 2006-09-11 | 2007-12-05 | 东南大学 | Hot-water type lithium bromide absorbing refrigerator between single effect and two stage |
| CN109163474A (en) * | 2018-10-16 | 2019-01-08 | 山东金佰瑞节能科技有限公司 | One pump multistage absorption-multistage evaporation absorption heat pump processed and the method for increasing the temperature difference |
| CN111174464A (en) * | 2020-01-06 | 2020-05-19 | 同方节能装备有限公司 | Double-effect double-energy water chilling unit |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| WO2022168460A1 (en) * | 2021-02-08 | 2022-08-11 | パナソニックＩｐマネジメント株式会社 | Evaporator unit for absorption refrigerator, heat exchange unit, and absorption refrigerator |
| EP4290165A4 (en) * | 2021-02-08 | 2024-04-10 | Panasonic Intellectual Property Management Co., Ltd. | Evaporator unit for absorption refrigerator, heat exchange unit, and absorption refrigerator |
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| CN112268382B (en) | 2024-04-30 |
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