CN112268382B - Novel circulation mode large-temperature-difference heat exchanger unit - Google Patents
Novel circulation mode large-temperature-difference heat exchanger unit Download PDFInfo
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- CN112268382B CN112268382B CN202011292822.3A CN202011292822A CN112268382B CN 112268382 B CN112268382 B CN 112268382B CN 202011292822 A CN202011292822 A CN 202011292822A CN 112268382 B CN112268382 B CN 112268382B
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- 239000006096 absorbing agent Substances 0.000 claims abstract description 126
- 239000003507 refrigerant Substances 0.000 claims abstract description 111
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 100
- 238000005507 spraying Methods 0.000 claims abstract description 35
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 claims abstract description 11
- 238000003860 storage Methods 0.000 claims description 21
- 239000007788 liquid Substances 0.000 claims description 14
- 238000000605 extraction Methods 0.000 claims description 10
- 239000007921 spray Substances 0.000 claims description 3
- 239000000243 solution Substances 0.000 description 118
- AMXOYNBUYSYVKV-UHFFFAOYSA-M lithium bromide Chemical group [Li+].[Br-] AMXOYNBUYSYVKV-UHFFFAOYSA-M 0.000 description 29
- 238000004519 manufacturing process Methods 0.000 description 12
- 238000010025 steaming Methods 0.000 description 10
- 239000000463 material Substances 0.000 description 8
- 238000001514 detection method Methods 0.000 description 7
- 238000010521 absorption reaction Methods 0.000 description 6
- 238000001704 evaporation Methods 0.000 description 5
- 238000005192 partition Methods 0.000 description 5
- 238000007789 sealing Methods 0.000 description 4
- 238000003466 welding 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
- 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
- 239000007864 aqueous solution 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
- 230000008020 evaporation Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
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
-
- 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
-
- 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
- F25B2500/00—Problems to be solved
- F25B2500/01—Geometry problems, e.g. for reducing size
-
- 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
Landscapes
- 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 mode large-temperature-difference heat exchanger unit; comprises a generator, a condenser, an evaporator group, an absorber group and a water-water plate heat exchanger; the generator is sequentially connected with the primary net water inlet, the water plate heat exchanger, the evaporator group and the primary net water outlet; the water-water plate 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 circulating mode large-temperature-difference heat exchanger unit.
Background
The lithium bromide unit is also called as lithium bromide absorption heat pump unit or large temperature difference heat supply unit, and is a device for preparing heating hot water under vacuum state by using heat network circulating water as heat source, water as refrigerant and lithium bromide aqueous solution as absorbent.
Disclosure of Invention
The invention aims to provide a novel circulating type large-temperature-difference heat exchanger unit, which solves the problems of the prior art, and has the advantages of simple structure, small heat exchange area and high heat exchange efficiency.
In order to achieve the above object, the present invention provides the following solutions:
the invention provides a novel circulation mode large-temperature-difference heat exchanger unit which comprises a generator, a condenser, an evaporator group, an absorber group and a 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 the first airtight 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 the second airtight equipment, the high-pressure absorber and the high-pressure evaporator are arranged in the third airtight equipment, the second airtight equipment is arranged above the third airtight equipment, and the second airtight equipment and the third airtight equipment are communicated and share one 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 plate type heat exchanger through a primary net water pipeline, the water plate type heat exchanger is communicated with the evaporator set through the primary net water pipeline, and the evaporator set is communicated with a primary net water outlet; the water-water plate 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 storage disc at the bottom of the low-pressure absorber is communicated with the high-pressure absorber through a pipeline, the solution storage disc 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 to spray, the refrigerant steam of the high-pressure evaporator is absorbed and finally is converged with solution in the solution storage disc 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, and the bottom of the generator is communicated with a second solution pipeline which 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 the 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 and converged with the second refrigerant pipeline through the pipeline and then is connected with a refrigerant pump, and the refrigerant pump is respectively 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 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; the secondary net water inlet is communicated with the low-pressure absorber and the high-pressure absorber in parallel through pipelines and then 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 the structure which is arranged up and down, only one solution storage disc is arranged at the bottom, the structure is simple, the amount of the solution which needs to be added by the unit is reduced, and the unit volume 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 second refrigerant pipelines, the refrigerant pump is respectively communicated with the spraying devices at the tops of the low-pressure evaporator and the high-pressure evaporator through third refrigerant pipelines, and the bottom of the condenser is converged with the branch of the high-pressure evaporator through the first refrigerant pipelines and the third refrigerant pipelines to be communicated with the spraying devices at the top of the high-pressure evaporator.
Optionally, the generator and the condenser are arranged in a first airtight device, the low-pressure absorber and the low-pressure evaporator are arranged in a second airtight device, the high-pressure absorber and the high-pressure evaporator are arranged in a third airtight device, and the second airtight device and the third airtight device are communicated and share a 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 set.
Compared with the prior art, the invention has the following technical effects:
Under the same working condition and the same load, the heat exchange area of the circulation mode is smaller than that of the traditional single-evaporation and single-absorption circulation mode, so that the volume of the unit is reduced, the whole solution amount is reduced, and the cost of the solution pump is reduced. Compared with the traditional double-steaming double-suction circulation mode, the upper cylinder is changed into a generator and a condenser from two generators and two condensers, and the lower cylinder is used for arranging the absorber and the evaporator in a second airtight device and a third airtight device which are communicated, so that only one set of air extraction system is needed, only one detection is needed when vacuum and the like are detected, the detection working time is reduced, and compared with the traditional double-steaming double-suction circulation mode, the structure reduces the unit cost from multiple aspects. Only one detection is needed, and the detection working time 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 is reduced by 55 percent, and the cost of the solution pump is further reduced. The total circulation amount of the lithium bromide solution can be reduced by 55% at most compared with the traditional double-evaporation double-absorption circulation mode, the required lithium bromide solution amount of a unit is reduced, and the unit cost is reduced; the electric appliance control system is changed from two sides to one side, the electric appliance control cost is reduced by about 30%, the electric appliance is reduced, and the material cost and the manufacturing time are reduced.
The invention sets the low-pressure absorber and the low-pressure evaporator in one closed device, the high-pressure absorber and the high-pressure evaporator in one closed device, and the two closed devices are connected up and down, thus reducing the cost of the machine set from many aspects and greatly reducing working procedures such as blanking and bending in the manufacturing process. The upper cylinder and the lower cylinder of the original double-steaming double-suction circulation mode structure are required to be divided into two independent cavities by the middle partition plate, the welding requirement on the partition plate is high, and the welding of the partition plate is subjected to leak-proof detection. 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%, the lithium bromide solution and the refrigerant amount are reduced, the piping material cost is reduced, the piping manufacturing cost is reduced, and the unit solution amount is reduced. The two sets of air extraction systems needed by the airtight equipment for placing the evaporator and the absorber are changed into one set, so that the manufacturing time and the material cost are reduced. The high-low pressure absorber is changed from a left-right structure to an upper-lower structure, the water tray of the absorber is reduced by half, the lithium bromide solution required by the liquid storage tray of the unit absorber is reduced by about 40%, and the solution cost is reduced. The water way pipe and the water chamber pipe avoid the difficult-to-operate cross pipe, and the aesthetic property, the manufacturing operability and the unit maintenance convenience of the water way pipe and the water chamber pipe are enhanced.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions of the prior art, the drawings that are needed in the embodiments will be briefly described below, it being obvious that the drawings in the following description are only some embodiments of the present invention, and that other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
FIG. 1 is a schematic diagram of a novel circulation mode large temperature difference heat exchanger unit structure;
wherein, 1 is the generator, 2 is the condenser, 3 is the steam circulation passageway, 4 is the primary network water inlet, 5 is the primary network water pipeline, 6 is the water plate heat exchanger, 7 is the primary network water export, 8 is the secondary network water pipeline, 9 is the secondary network water inlet, 10 is the secondary network water export, 11 is first solution pipeline, 12 is solution heat exchanger, 13 is the second solution pipeline, 14 is the solution pump, 15 is first refrigerant pipeline, 16 is the second refrigerant pipeline, 17 is the refrigerant pump, 18 is the third refrigerant pipeline, 19 is low pressure absorber, 20 is high pressure absorber, 21 is low pressure evaporator, 22 is high pressure evaporator, 23 is the third solution pipeline.
Detailed Description
The following description of the embodiments of the present invention will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present invention, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.
The invention aims to provide a novel circulating type large-temperature-difference heat exchanger unit, which solves the problems of the prior art, and has the advantages of simple structure, small heat exchange area and high heat exchange efficiency.
In order that the above-recited objects, features and advantages of the present invention will become more readily apparent, a more particular description of the invention will be rendered by reference to the appended drawings and appended detailed description.
The traditional large-temperature-difference heat exchanger unit mainly comprises a single-steaming single-suction circulation mode structure and a double-steaming double-suction circulation mode structure; based on the fact that the traditional heat exchange structure has certain defects, the invention provides a novel circulating type large-temperature-difference heat exchange unit, which is shown in figure 1 and comprises a generator 1, a condenser 2, an evaporator group, an absorber group and a water plate heat exchanger 6; 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 plate heat exchanger 6 through a primary net water pipeline 5, the water plate 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 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 the 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 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 set, the bottom of the evaporator set 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 set 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 equipment, 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 the second airtight equipment, the high-pressure absorber 20 and the high-pressure evaporator 22 are arranged in the third airtight equipment, the second airtight equipment is arranged above the third airtight equipment, 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 airtight equipment and the third airtight equipment share a set of pumping 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; only one solution storage disc is arranged at the bottom of the low-pressure absorber 19 and the high-pressure absorber 20, and only one refrigerant storage disc is arranged at the bottom of the low-pressure evaporator 21 and the high-pressure evaporator 22. The solution storage disc at the bottom of the high-pressure absorber 20 is connected with a first solution pipeline 11, the first solution pipeline 11 is provided with a solution pump 14, concentrated solution in the low-pressure absorber 19 absorbs refrigerant steam of the low-pressure evaporator and then becomes intermediate solution to enter the high-pressure absorber 20 for spraying, meanwhile, solution after absorbing the refrigerant steam of the high-pressure evaporator and solution in the solution storage disc of the high-pressure absorber 20 are combined and then enter the solution heat exchanger 12 through the 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 the 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.
Further preferably, the low pressure absorber 19 is arranged above the high pressure absorber 20, so that only one solution storage tray is arranged at the bottom of the absorber group; 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 heat exchanger 6 is connected with the high-pressure evaporator 22 and the low-pressure evaporator 21 in series through a 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 connected in series with the condenser 2 and the secondary net water outlet 10 after being communicated with the low-pressure absorber 19 and the high-pressure absorber 20 in parallel through pipelines. 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 the 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 a 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 a 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 the refrigerant pump 17 through the second refrigerant pipeline 16, 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 the third refrigerant pipeline 18, and the bottom of the condenser 2 is communicated with the spraying devices at the tops of the high-pressure evaporator 22 after being converged with the branches from the third refrigerant pipeline 18 to the high-pressure evaporator 22 through the 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 a set of air extraction system. The absorber group and the evaporator group can be made into an integral water chamber structure, the structure is simpler, and the cross piping difficult to operate is avoided.
In the invention, the high and low pressure sides of the lithium bromide solution are in series connection, and the cycle mode is as follows:
Lithium bromide solution side: the dilute solution enters the solution heat exchanger from the high-pressure absorber through the solution pump to exchange heat with the concentrated solution, then enters the generator, the concentrated solution is concentrated into the concentrated solution, the concentrated solution enters the solution heat exchanger from the generator to exchange heat with the dilute solution, then enters the low-pressure absorber to spray, the concentrated solution absorbs the refrigerant steam of the low-pressure evaporator to dilute into intermediate solution, the intermediate solution enters the high-pressure absorber to absorb the refrigerant steam generated by the high-pressure evaporator to dilute into the dilute solution, and the dilute solution is continuously circulated, so that the vacuum degree of the whole circulation loop can be monitored and controlled only by one set of metering device system.
Refrigerant side: the generator condenses the dilute solution to generate refrigerant steam, and the refrigerant steam enters the condenser to generate refrigerant water. The refrigerant water in the condenser directly enters the spraying device of the high-pressure evaporator to be sprayed, does not enter the water disc of the evaporator to flash, enters the spraying device of the high-pressure evaporator to be sprayed and then reaches the spraying device of the evaporator group to be sprayed through the refrigerant pump, so that the circulation quantity of the refrigerant circulating pump is reduced; the model of the refrigerant pump is reduced, the residual refrigerant water sprayed by the low-pressure evaporator is converged at the refrigerant outlet of the liquid storage disc of the high-pressure evaporator through the second refrigerant pipeline, and then the residual refrigerant water is sprayed by the refrigerant pump through two paths of spraying devices respectively entering the low-pressure evaporator and the high-pressure evaporator, so that one refrigerant pump is reduced, and the whole volume of the equipment is reduced.
The refrigerant water in the liquid storage disc of the high-pressure evaporator is delivered to the low-pressure evaporator to be sprayed and evaporated through a refrigerant pump to generate refrigerant steam, the refrigerant steam is absorbed by the concentrated solution of the low-pressure absorber through a steam flow channel 3, the concentrated solution becomes intermediate liquid, the other path of refrigerant steam and the refrigerant water in the condenser are delivered to a dispersing device of the high-pressure generator to be sprayed and evaporated to generate refrigerant steam, the refrigerant steam is absorbed by the intermediate liquid of the high-pressure absorber through the steam flow channel 3, the intermediate liquid becomes dilute solution, and the dilute solution continues to circulate. The low pressure evaporator and the low pressure absorber are connected by one 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 water: the primary net water is cooled once through the generator, continuously enters the water plate heat exchanger and the secondary net water for secondary cooling, continuously enters the high-pressure evaporator for tertiary cooling, continuously enters the low-pressure evaporator for quaternary cooling, and finally enters the demand area from the low-pressure evaporator.
And the secondary net water is two paths of secondary net water, one path of the secondary net water enters the water-water plate heat exchanger to exchange heat with the primary net water, the other path of the secondary net water is divided into two paths to be respectively heated to the high-pressure absorber and the low-pressure absorber for one time, and then the two paths of the secondary net water enter the condenser to be heated for the second time, and the secondary net water from the water-water plate heat exchanger and the secondary net water from the condenser are combined into one path of water to enter a required area.
The circulation mode of the invention is compared with the traditional single-steaming and single-absorbing circulation mode:
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 and double-suction circulation mode, the circulation mode of the heat exchange unit provided by the invention is as follows:
under the same working condition and the same load. The circulation mode of the invention has the advantages that the upper sealing device (high temperature cylinder) is changed into a generator and a condenser from two generators and two condensers, and the lower sealing device (low temperature cylinder) is combined into a communicated device by two independent evaporation and absorption cylinders, so that the structure reduces the unit cost from multiple aspects.
Specifically, the invention has the following advantages:
1. Material cost reduction
The lower cylinder body of the sealing equipment is narrowed and heightened, 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 made of corrugated plates which are thinner than the upper and lower barrel plates and 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 circulation quantity of the solution and the refrigerant is reduced by 55 percent, the types of the solution pump and the refrigerant pump can be selected to be small, and the cost is further reduced.
The total circulation amount of the lithium bromide solution can be reduced by 55% at most compared with the traditional single-evaporation single-absorption and double-evaporation double-absorption circulation modes, the amount of the lithium bromide solution required by a machine set is reduced, and the cost of the lithium bromide solution is reduced.
The solution piping and refrigerant piping of the solution pump base, the refrigerant pump unit and the like are changed from two side piping to one side piping, the piping is reduced by 30%, the piping material cost is reduced, the lithium bromide solution and refrigerant cost is reduced, and the piping 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 disc is reduced by half, the lithium bromide solution required by the unit absorber liquid storage disc is reduced by about 40%, and the solution cost is reduced.
The second airtight equipment with the low-pressure absorber and the low-pressure evaporator, the high-pressure absorber and the third airtight equipment with the high-pressure evaporator adopt an up-down structure, so that the vacuum environment requirement required by the whole unit can be met by only one set of air extraction system, the two sets of air extraction systems are changed into one set, and the material cost is reduced
The electric appliance control system is changed from two sides to one side, the electric appliance control cost is reduced by about 30%, the electric appliance is reduced, and the material cost is reduced.
2. Manufacturing cost reduction
The upper cylinder and the lower cylinder of the sealing device are respectively combined into one cylinder by two independent cylinders, so that the working procedures of blanking, bending and the like in the manufacturing process are reduced.
The upper cylinder and the lower cylinder of the original double-steaming and double-sucking circulation mode structure respectively need the middle partition plate to be divided into two independent cavities, and the welding requirements on the partition plate are high
The high-pressure water chamber and the low-pressure water chamber of the original double-steaming double-suction circulation mode structure unit are independently manufactured, the number of the high-pressure water chamber, the low-pressure absorber and the evaporator water chamber of the circulation mode generator is changed from two to one, and the number of the water chambers is reduced by half.
When the vacuum and other detection of the original double-steaming double-suction circulation type structural unit are carried out, one side is required to be detected firstly on the high-pressure side and the low-pressure side, then the other side is required to be detected, and the detection working hours are more.
The solution pump base, the solution piping of the refrigerant pump unit and the like and the refrigerant piping are changed from two side piping to one side piping, the piping is reduced by 30%, and the manufacturing cost of the piping is reduced.
The two sets of air extraction systems are changed into one set, so that the manufacturing time is reduced.
The electric appliance control system is changed from two sides to one side, so that the manufacturing time is reduced.
3. Appearance and others
The invention has more compact overall structure, particularly occupies less space in the width direction, and has wider applicability to the field space of clients.
The electric appliance control system is changed from two sides to one side, the control points are reduced, the junction boxes and wiring pipelines are reduced, and the whole appearance of the unit is more concise.
The water way pipe and the water chamber pipe avoid the difficult-to-operate cross pipe, and the aesthetic property, the manufacturing operability and the unit maintenance convenience of the water way pipe and the water chamber pipe are enhanced.
The principles and embodiments of the present invention have been described in detail with reference to specific examples, which are provided to facilitate understanding of the method and core ideas of the present invention; also, it is within the scope of the present invention to be modified by those of ordinary skill in the art in light of the present teachings. In view of the foregoing, this description should not be construed as limiting the invention.
Claims (5)
1. A novel circulation mode large temperature difference heat exchanger unit is characterized in that: the device comprises a generator, a condenser, an evaporator set, an absorber set and a water-water plate type heat exchanger, wherein the absorber set comprises a low-pressure absorber and a high-pressure absorber, and the evaporator set comprises a low-pressure evaporator and a high-pressure evaporator; the generator and the condenser are arranged in the first airtight 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 the second airtight equipment, the high-pressure absorber and the high-pressure evaporator are arranged in the third airtight equipment, the second airtight equipment is arranged above the third airtight equipment, and the second airtight equipment and the third airtight equipment are communicated and share one 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 plate type heat exchanger through a primary net water pipeline, the water plate type heat exchanger is communicated with the evaporator set through the primary net water pipeline, and the evaporator set is communicated with a primary net water outlet; the water-water plate 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 disc 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 steam of the low-pressure evaporator enters the high-pressure absorber to spray, the intermediate liquid absorbs the refrigerant steam of the high-pressure evaporator and finally merges with the solution in the solution storage disc 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, and a second solution pipeline is communicated with a 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 the 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 and converged with the second refrigerant pipeline through the pipeline and then is connected with a refrigerant pump, and the refrigerant pump is respectively communicated with the spraying devices at the tops of the low-pressure evaporator and the high-pressure evaporator through a third refrigerant pipeline; the water-water plate 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; the secondary net water inlet is communicated with the low-pressure absorber and the high-pressure absorber in parallel through pipelines and then connected with the condenser and the secondary net water outlet in series; the high-pressure absorber bottom is connected with a first solution pipeline, 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, the second solution pipeline is connected with a 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.
2. The novel circulation mode large temperature difference heat exchanger unit according to claim 1, wherein: 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 spraying devices at the tops of the low-pressure evaporator and the high-pressure evaporator through third refrigerant pipelines, and the condenser bottom is converged with the branch of the high-pressure evaporator through the first refrigerant pipelines and the branch of the third refrigerant pipelines to be communicated with the spraying devices at the top of the high-pressure evaporator.
3. The novel circulation mode large temperature difference heat exchanger unit according to claim 1, wherein: the generator and the condenser are arranged in the first airtight equipment, the low-pressure absorber and the low-pressure evaporator are arranged in the second airtight equipment, the high-pressure absorber and the high-pressure evaporator are arranged in the third airtight equipment, and the second airtight equipment and the third airtight equipment are communicated and share one set of air extraction system.
4. The novel circulation mode large temperature difference heat exchanger unit according to claim 1, wherein: 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.
5. The novel circulation mode large temperature difference heat exchanger unit according to claim 1, wherein: the solution pump is disposed between the solution heat exchanger and the absorber set.
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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 true CN112268382B (en) | 2024-04-30 |
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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
- 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 |
| 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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