CN117287872A - Composite condensation evaporator and application thereof - Google Patents
Composite condensation evaporator and application thereof Download PDFInfo
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- CN117287872A CN117287872A CN202311581139.5A CN202311581139A CN117287872A CN 117287872 A CN117287872 A CN 117287872A CN 202311581139 A CN202311581139 A CN 202311581139A CN 117287872 A CN117287872 A CN 117287872A
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- 238000009833 condensation Methods 0.000 title claims abstract description 59
- 230000005494 condensation Effects 0.000 title claims abstract description 59
- 239000002131 composite material Substances 0.000 title claims abstract description 57
- 238000005057 refrigeration Methods 0.000 claims abstract description 57
- 238000010521 absorption reaction Methods 0.000 claims abstract description 40
- 238000000034 method Methods 0.000 claims abstract description 26
- 230000008569 process Effects 0.000 claims abstract description 18
- 238000007789 sealing Methods 0.000 claims abstract description 11
- 239000007788 liquid Substances 0.000 claims description 127
- 239000003507 refrigerant Substances 0.000 claims description 114
- 229920006395 saturated elastomer Polymers 0.000 claims description 45
- 239000006096 absorbing agent Substances 0.000 claims description 35
- 238000001704 evaporation Methods 0.000 claims description 13
- 238000010992 reflux Methods 0.000 claims description 12
- 230000008020 evaporation Effects 0.000 claims description 10
- 230000009471 action Effects 0.000 claims description 9
- 238000010168 coupling process Methods 0.000 claims description 3
- 238000010438 heat treatment Methods 0.000 claims description 3
- 239000007789 gas Substances 0.000 description 62
- 239000000243 solution Substances 0.000 description 29
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 10
- 238000005265 energy consumption Methods 0.000 description 6
- 238000001816 cooling Methods 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 230000006872 improvement Effects 0.000 description 4
- 239000000463 material Substances 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- 239000012808 vapor phase Substances 0.000 description 2
- 239000002918 waste heat Substances 0.000 description 2
- 230000006978 adaptation Effects 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 238000005272 metallurgy Methods 0.000 description 1
- 239000011259 mixed solution Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000005514 two-phase flow Effects 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
- F25B39/00—Evaporators; Condensers
- F25B39/02—Evaporators
- F25B39/026—Evaporators specially adapted for sorption type systems
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/32—Other features of fractionating columns ; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0003—Condensation of vapours; Recovering volatile solvents by condensation by using heat-exchange surfaces for indirect contact between gases or vapours and the cooling medium
- B01D5/0009—Horizontal tubes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0033—Other features
- B01D5/0039—Recuperation of heat, e.g. use of heat pump(s), compression
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0057—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes
- B01D5/006—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes with evaporation or distillation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0078—Condensation of vapours; Recovering volatile solvents by condensation characterised by auxiliary systems or arrangements
- B01D5/0087—Recirculating of the cooling medium
-
- 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
- F25B15/04—Sorption machines, plants or systems, operating continuously, e.g. absorption type without inert gas the refrigerant being ammonia evaporated from aqueous solution
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
- F28D7/0066—Multi-circuit heat-exchangers, e.g. integrating different heat exchange sections in the same unit or heat-exchangers for more than two fluids
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F9/00—Casings; Header boxes; Auxiliary supports for elements; Auxiliary members within casings
- F28F9/02—Header boxes; End plates
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Sorption Type Refrigeration Machines (AREA)
Abstract
The invention belongs to the technical field of absorption refrigeration and rectification, and particularly relates to a composite condensation evaporator and application thereof, wherein the composite condensation evaporator comprises a cylinder body and sealing heads positioned at two ends of the cylinder body, and two outer tube plates and two inner tube plates are symmetrically arranged in the cylinder body from outside to inside; a plurality of inner heat exchange tubes are uniformly distributed between the two outer tube plates, and two ends of each inner heat exchange tube are respectively communicated with sealing heads at two ends of the cylinder; a plurality of outer heat exchange tubes are uniformly distributed between the two inner tube plates; the middle section of the inner heat exchange tube is positioned inside the outer heat exchange tube. The invention embeds the absorption refrigeration system in the rectification system by the special design of the composite condensation evaporator structure, and couples the rectification and refrigeration processes. Meanwhile, the special design of the composite condensation evaporator structure optimizes the inside of the refrigeration process, thereby further improving the refrigeration and rectification efficiency.
Description
Technical Field
The invention belongs to the technical field of absorption refrigeration and rectification, and particularly relates to a composite condensation evaporator and application thereof.
Background
The rectification is a distillation method for obtaining high-purity separation by mixing liquid by reflux, is the most widely applied liquid mixture separation operation in industry, and is widely applied to the departments of petroleum, chemical industry, light industry, food, metallurgy and the like. Typical rectification apparatus are continuous rectification apparatus (as shown in figure 1) including rectification columns, reboilers, condensers and the like. The rectifying tower is used for carrying out phase-to-phase mass transfer by contacting vapor with liquid phase, a condenser positioned at the top of the rectifying tower is used for partially condensing vapor, partial condensate is used as reflux liquid and returns to the top of the rectifying tower, and the rest distillate is the product at the top of the rectifying tower. A reboiler at the bottom of the column vaporizes a portion of the liquid, with the vapor rising along the column and the remaining liquid as a bottom product. Most of condensers at the top of the tower adopt circulating water as a cooling medium, and the consumption of the circulating water is large due to the large amount of cold energy required by the condensers, so that the energy consumption of public works is increased. In summer, the temperature of circulating water is high, so that the condensing pressure at the top of the rectifying tower is too high, more heat is required to be input into a reboiler at the bottom of the rectifying tower, and energy consumption is increased.
The absorption refrigeration system utilizes low-grade waste heat to drive a thermodynamic working medium, and performs refrigeration through phase change of the working medium (such as ammonia). The main equipment comprises a generator, a condenser, an evaporator, an absorber, a solution pump and the like. As shown in fig. 2, the low-grade waste heat is used to heat the mixed solution (rich solution for short) with a certain concentration and rich in the refrigerant, which is conveyed from the absorber by the solution pump, so that most of the low-boiling-point refrigerant in the rich solution is desorbed, and is changed into high-pressure gaseous refrigerant, which enters the condenser, and is cooled into high-pressure liquid refrigerant by circulating water, the high-pressure liquid refrigerant is decompressed into low-pressure gas-liquid saturated state refrigerant by the expansion valve, the low-pressure gas-liquid saturated state refrigerant enters the evaporator, the heat of the medium to be cooled is absorbed and is vaporized into low-pressure gaseous refrigerant, and the low-pressure gaseous refrigerant enters the absorber. The residual high-pressure lean solution in the generator is decompressed into low-pressure lean solution by a decompression valve, enters an absorber, is mixed with low-pressure gaseous refrigerant from an evaporator for absorption, is recovered to the original concentration, becomes normal-temperature rich solution, is boosted by a solution pump and is then sent into the generator for continuous circulation. In the above operation, flash-off tends to occur due to adiabatic throttling and depressurization. The high-pressure liquid refrigerant is throttled and decompressed by the expansion valve to become low-pressure gas-liquid saturated refrigerant, if the low-pressure gas-liquid saturated refrigerant can be separated out before entering the evaporator, the pure liquid low-pressure saturated refrigerant enters the evaporator, and the evaporation efficiency can be greatly improved, because the evaporation efficiency of the saturated gas-liquid two-phase flow is lower than that of the saturated pure liquid phase flow. In addition, since the normal temperature rich liquid coming out of the absorber is already close to the saturation state, cavitation of the solution pump is extremely easily caused when the normal temperature rich liquid enters the solution pump. It is conventional practice to increase the height difference between the absorber and the solution pump to increase the effective cavitation margin. The overall height of the unit is increased, the cost of the unit pipeline is increased, and meanwhile, the cost is increased for ultra-high transportation.
Therefore we propose a composite condensation evaporator and its application to solve the above problems.
Disclosure of Invention
In order to solve the problems, a composite condensation evaporator and application thereof are provided.
The above object is achieved by the following preparation process:
the first object of the invention is to provide a composite condensation evaporator, which comprises a cylinder body and sealing heads positioned at two ends of the cylinder body, wherein two outer tube plates and two inner tube plates are symmetrically arranged in the cylinder body from outside to inside; a first shell-pass cylinder is arranged between one outer tube plate and the inner tube plate, a third shell-pass cylinder is arranged between the other outer tube plate and the inner tube plate, and a second shell-pass cylinder is arranged between the two inner tube plates;
a plurality of inner heat exchange tubes are uniformly distributed between the two outer tube plates, and two ends of each inner heat exchange tube are respectively communicated with sealing heads at two ends of the cylinder; a plurality of outer heat exchange tubes are uniformly distributed between the two inner tube plates, and two ends of each outer heat exchange tube are respectively communicated with the first shell side cylinder and the third shell side cylinder; the middle section of the inner heat exchange tube is positioned inside the outer heat exchange tube;
an outer jacket is arranged on the outer side of the second shell-side cylinder, and a group of swirl plates are welded and fixed between the outer jacket and the second shell-side cylinder;
one of the sealing heads is provided with a medium inlet, and the other sealing head is provided with a medium outlet; the third shell-side cylinder is provided with a low-pressure gas-liquid saturated medium inlet and a low-pressure gas medium first outlet, the first shell-side cylinder is provided with a low-pressure gas medium second outlet, the outer jacket is provided with a low-pressure gas medium inlet and a low-pressure gas medium second outlet at the head and the tail of the cyclone plate, and the second shell-side cylinder is provided with a gas inlet and a condensate outlet.
As a further improvement of the technical scheme, the low-pressure gas-liquid saturated medium inlet is positioned at the upper side surface of the third shell-side cylinder.
As a further improvement of the technical scheme, the operation process of the composite condensation evaporator is as follows:
the first medium circulates in the inner heat exchange tube, and the initial form of the first medium is normal-temperature medium; the third shell-side cylinder, the outer heat exchange tube, the first shell-side cylinder and the outer jacket are sequentially communicated with a second medium, and the initial form of the second medium is a low-pressure low-temperature gas-liquid saturated state; the second shell-side cylinder body circulates a third medium, and the initial form of the third medium is a high-temperature medium; the specific heat exchange process of the three media is as follows:
after the second medium in the low-pressure gas-liquid saturated state enters the third shell-pass cylinder, one part of the second medium is flashed to form a low-pressure gas medium which flows out from the first outlet of the low-pressure gas medium, the other part of the flashed low-pressure liquid medium downwards enters a cavity between the outer heat exchange tube and the inner heat exchange tube, absorbs the heat of the third medium outside the outer heat exchange tube and the heat of the first medium inside the inner heat exchange tube, is gasified into the low-pressure gas medium, is then introduced into the outer jacket, absorbs the heat of the first medium again under the swirling action of the swirling plate, and the low-pressure gas medium after secondary utilization flows out from the second outlet of the low-pressure gas medium and is merged with the low-pressure gas medium flowing out from the first outlet of the low-pressure gas medium to participate in the next flow;
after the first medium absorbs heat, the first medium becomes a supercooled medium and participates in the next process;
after the third medium absorbs heat, the third medium is condensed into a liquid state to participate in the next process.
As a further improvement of the technical scheme, the operation process of the composite condensation evaporator is as follows:
the first medium is normal-temperature rich liquid from the absorber, the second medium is low-pressure low-temperature gas-liquid saturated refrigerant which is from the condenser and passes through the expansion valve, and the third medium is tower top gas from the top of the rectifying tower;
after the low-pressure gas-liquid saturated refrigerant enters the third shell-side cylinder, part of the low-pressure gas-state refrigerant is flashed to form low-pressure gas-state refrigerant which flows out from the first outlet of the low-pressure gas-state refrigerant, and the other part of the flashed low-pressure liquid-state refrigerant downwards enters a cavity between the outer heat exchange tube and the inner heat exchange tube; the tower top gas from the rectifying tower enters a second shell-side cylinder from a gas inlet, and the normal-temperature rich liquid from the absorber enters an inner heat exchange tube;
the low-pressure liquid refrigerant after flash evaporation downwards enters a cavity between the outer heat exchange tube and the inner heat exchange tube, absorbs heat of tower top gas outside the outer heat exchange tube and normal-temperature rich liquid inside the inner heat exchange tube, is gasified into low-pressure gaseous refrigerant, is then introduced into an outer jacket, absorbs heat of the tower top gas again under the swirling action of a swirling plate, and cold energy is converged with the low-pressure gaseous refrigerant flowing out of a first outlet of the low-pressure gaseous refrigerant from a second outlet of the low-pressure gaseous refrigerant after secondary utilization, and enters an absorber to continue refrigeration cycle;
after the normal-temperature rich liquid in the inner heat exchange tube is absorbed by heat, the normal-temperature rich liquid becomes a low-temperature rich liquid in a supercooled state, and then the solution pump is removed to continue the refrigeration cycle;
the tower top gas outside the outer heat exchange tube is condensed into liquid after absorbing heat, one part is taken as tower top product condensate liquid, and the other part is taken as tower top reflux liquid and enters the rectifying tower for rectifying operation.
As a further improvement of the technical scheme, a plurality of baffle plates are arranged on the outer side of the outer heat exchange tube.
The second object of the invention is to provide a rectification system, which comprises a rectification tower and a reboiler, and further comprises the composite condensation evaporator for replacing a condenser in the existing rectification system, wherein the top gas of the rectification tower enters into a second shell side cylinder of the composite condensation evaporator to exchange heat with a medium in an outer heat exchange pipe and an outer jacket to form a top condensate, one part of the top condensate is collected, and the other part of the top condensate is taken as top reflux.
The third object of the invention is to provide an absorption refrigeration system, which comprises an absorber, a solution pump, a generator and a condenser, and further comprises the composite condensation evaporator for replacing the evaporator in the existing absorption refrigeration system, wherein an expansion valve is arranged between the condenser and the composite condensation evaporator, and high-pressure liquid refrigerant in the condenser passes through the expansion valve to form low-pressure gas-liquid saturated refrigerant;
after the low-pressure gas saturated state refrigerant enters the third shell side cylinder of the composite condensation evaporator, part of the low-pressure gas refrigerant is flashed to form low-pressure gas refrigerant to flow out from the first outlet of the low-pressure gas refrigerant, the other part of the flashed low-pressure liquid refrigerant enters a cavity between the outer heat exchange tube and the inner heat exchange tube downwards, the heat of the tower top gas outside the outer heat exchange tube and the normal-temperature rich liquid inside the inner heat exchange tube is absorbed, the low-pressure gas refrigerant is gasified to be low-pressure gas refrigerant, the low-pressure gas refrigerant is introduced into an outer jacket, the heat of the tower top gas is absorbed again under the swirling action of a swirling plate, the cold energy is converged by the low-pressure gas refrigerant which flows out from the second outlet of the low-pressure gas refrigerant and flows out from the first outlet of the low-pressure gas refrigerant, and the low-pressure gas refrigerant flows into an absorber, and the refrigeration cycle is continued;
the normal temperature rich liquid from the absorber enters the inner heat exchange tube, the normal temperature rich liquid in the inner heat exchange tube is absorbed by heat and becomes the low temperature rich liquid in a supercooled state, and then the low temperature rich liquid is pumped into the generator by the solution pump to continue the refrigeration cycle.
The fourth object of the present invention is to provide an absorption condensation rectification system, which comprises the rectification system and the absorption refrigeration system, wherein the composite condensation evaporator in the rectification system and the composite condensation evaporator in the absorption refrigeration system are in the same group, and a steam condensate outlet of the reboiler is connected with a heat source inlet of the generator, and is used for taking the steam condensate coming out of the reboiler of the rectification system as a heat source for driving the absorption refrigeration system.
The fifth object of the present invention is to provide a rectification and refrigeration coupling process, which utilizes the above-mentioned absorption condensation rectification system, comprising the following steps:
a rectifying tower, a reboiler and a pipeline of a composite condensation evaporator of the rectifying system are communicated, and a tower bottom gas-liquid circulation is established;
the method comprises the steps of (1) opening a heat source pipeline of a generator of an absorption refrigeration system, introducing a heat source discharged by a reboiler, heating, raising the temperature and the pressure of the generator, evaporating gaseous refrigerant in a working medium solution to generate the generator, condensing the gaseous refrigerant in the condenser, enabling the condensed high-pressure liquid refrigerant to pass through an expansion valve to obtain low-pressure gas-liquid saturated refrigerant, enabling the low-pressure gas-liquid saturated refrigerant to enter the composite condensation evaporator to exchange heat with the top gas of a rectifying tower, enabling the top gas to form a top condensate, enabling one part of the top gas to be collected, enabling the other part of the top gas to serve as top reflux liquid, establishing top gas-liquid circulation of the rectifying system, enabling the gas-liquid saturated refrigerant to evaporate to form gaseous refrigerant to enter the absorber, and enabling the solution of the absorber to be mixed and pumped into the generator through the solution pump, so as to establish refrigerant circulation.
The invention has the beneficial effects that:
(1) And taking the steam condensate from the reboiler of the rectification system as a heat source for driving the absorption refrigeration system, namely introducing the steam condensate from the reboiler into a generator in the absorption refrigeration system, and preparing cold energy for a condenser in the rectification system by driving a thermodynamic working medium. The heat in the steam condensate discharged from the reboiler is recycled, so that the utilization rate of energy sources can be improved. Meanwhile, the cold energy produced by the refrigerating unit is used for cooling a condenser in the rectification system to replace the original circulating water, so that the consumption of the circulating water is reduced, and the energy consumption of public engineering is reduced. In addition, the temperature of the produced cold quantity is lower than that of the circulating water, so that the condensing pressure at the top of the rectifying tower can be reduced, the heat input at the bottom of the tower can be further reduced, and the energy consumption is reduced.
(2) The vapor phase in the low-pressure state vapor-liquid saturated state refrigerant before entering the evaporator is separated, so that the evaporation efficiency can be greatly improved. And meanwhile, partial cold energy in the evaporator is used for cooling the normal-temperature rich liquid from the absorber to enable the normal-temperature rich liquid to be in a supercooled state, so that the normal-temperature rich liquid enters the solution pump, and cavitation of the solution pump can be avoided. The method replaces the original method (increases the height difference between the absorber and the solution pump), can reduce the cost of a unit pipeline, and simultaneously reduces the cost for ultra-high transportation.
(3) The special design of the composite condensing evaporator structure embeds the absorption refrigeration system in the rectification system, and couples the rectification and refrigeration processes. Meanwhile, the special design of the composite condensation evaporator structure optimizes the refrigeration process internally, thereby further improving the refrigeration and rectification efficiency.
Drawings
FIG. 1 is a schematic diagram of the overall flow of a continuous rectification apparatus in the prior art;
FIG. 2 is a schematic diagram of the overall flow of an absorption refrigeration system of the prior art;
FIG. 3 is a schematic flow chart of a composite condensation evaporator according to example 1 of the present invention;
FIG. 4 is a schematic cross-sectional view of a composite condensation evaporator according to the present invention;
FIG. 5 is a schematic flow chart of a composite condensation evaporator in example 2 of the present invention;
fig. 6 is a schematic diagram of the overall flow of the absorption condensing and rectifying system in the present invention, wherein the left half part is the rectifying system, and the right half part is the absorption refrigerating system.
The diagram is: 1. a cylinder; 2. an inner heat exchange tube; 3. an outer heat exchange tube; 4. an outer jacket; 5. a swirl plate; 6. a baffle.
Detailed Description
The following detailed description of the present application is provided in conjunction with the accompanying drawings, and it is to be understood that the following detailed description is merely illustrative of the application and is not to be construed as limiting the scope of the application, since numerous insubstantial modifications and adaptations of the application will be to those skilled in the art in light of the foregoing disclosure.
Example 1
As shown in fig. 3 to 5, the composite condensation evaporator of the present embodiment has a main structure of a cylinder 1, the inside of which is composed of two parts of an inner tube bundle and an outer tube bundle, and each inner heat exchange tube of the inner tube bundle is inserted into each outer heat exchange tube of the outer tube bundle. The two ends of each outer heat exchange tube are welded and fixed on the inner tube plates A1 and A2, a plurality of baffle plates are fixed in the middle area of each outer heat exchange tube, and the two ends of each inner heat exchange tube are welded and fixed on the outer tube plates B1 and B2. The shell-pass type cyclone separator comprises a cylinder body 1, wherein a first shell-pass cylinder body C1 is arranged between one outer tube plate B1 and an inner tube plate A1, a third shell-pass cylinder body C3 is arranged between the other outer tube plate B2 and the inner tube plate A2, a second shell-pass cylinder body C2 is arranged between the inner tube plate A1 and the inner tube plate A2, sealing heads D1 and D2 are respectively welded and fixed on the outer tube plate B1 and the outer tube plate B2, an outer jacket is welded and fixed on the second shell-pass cylinder body C2, and a group of cyclone plates are welded and fixed between the outer jacket and the shell-pass cylinder body C2.
A medium inlet is formed in the end socket D1, and a medium outlet is formed in the end socket D2; the third shell-side cylinder C3 is provided with a low-pressure gas-liquid saturated state medium inlet and a low-pressure gas-liquid saturated state medium first outlet, the low-pressure gas-liquid saturated state medium inlet is positioned on the upper side surface of the third shell-side cylinder C3, the first shell-side cylinder C1 is provided with a low-pressure gas-medium second outlet, the outer jacket 4 is provided with a low-pressure gas-medium inlet and a low-pressure gas-medium second outlet at the head and the tail of the cyclone plate 5 respectively, and the second shell-side cylinder C2 is provided with a gas inlet and a condensate outlet respectively.
As shown in fig. 3, the operation process of the above-mentioned composite condensation evaporator is as follows:
the first medium flows through the inner heat exchange tube 2, and the initial form of the first medium is normal-temperature medium; the third shell-side cylinder C3, the outer heat exchange tube 3, the first shell-side cylinder C1 and the outer jacket 4 are sequentially communicated with a second medium, and the initial form of the second medium is a low-pressure low-temperature gas-liquid saturated state; the second shell side cylinder C2 is communicated with a third medium, and the initial form of the third medium is a high-temperature medium; the specific heat exchange process of the three media is as follows:
after the second medium in the low-pressure gas-liquid saturated state enters the third shell-pass cylinder C3, one part of the second medium is flashed to form a low-pressure gas medium which flows out from the first outlet of the low-pressure gas medium, the other part of the flashed low-pressure liquid medium downwards enters a cavity between the outer heat exchange tube 3 and the inner heat exchange tube 2, absorbs the heat of the third medium outside the outer heat exchange tube 3 and the first medium inside the inner heat exchange tube 2, is gasified into the low-pressure gas medium, is then introduced into the outer jacket 4, absorbs the heat of the third medium again under the swirling action of the swirling flow plate 5, and the cold energy is converged by the low-pressure gas medium which flows out from the second outlet of the low-pressure gas medium after secondary use and the low-pressure gas medium which flows out from the first outlet of the low-pressure gas medium to participate in the next flow;
after the first medium absorbs heat, the first medium becomes a supercooled medium and participates in the next process;
after the third medium absorbs heat, the third medium is condensed into a liquid state to participate in the next process.
Example 2
As shown in fig. 5, when the first medium is normal temperature rich liquid from an absorber (absorption refrigeration system), the second medium is condenser absorption refrigeration system, the low pressure low temperature gas-liquid saturated refrigerant after passing through the expansion valve, and the third medium is tower top gas from the top of the rectifying tower (rectifying system);
after the low-pressure gas-liquid saturated refrigerant enters the third shell-side cylinder C3, as the material flow enters the large space of the shell-side cylinder C3 from the small space of the connecting pipe, the large space of the third shell-side cylinder C3 provides a space for flash evaporation separation of the material flow, one part of the material flow is flash evaporated to form the low-pressure gas refrigerant to flow out from the first outlet of the low-pressure gas refrigerant, and the other part of the low-pressure liquid refrigerant after flash evaporation enters the cavity between the outer heat exchange tube 3 and the inner heat exchange tube 2 downwards; the tower top gas from the rectifying tower enters a second shell-side cylinder C2 from a gas inlet, and normal-temperature rich liquid from the absorber enters an inner heat exchange tube 2;
the low-pressure liquid refrigerant after flash evaporation enters the cavity between the outer heat exchange tube 3 and the inner heat exchange tube 2 downwards, absorbs heat of tower top gas outside the outer heat exchange tube 3 and normal-temperature rich liquid inside the inner heat exchange tube 2, is gasified into low-pressure gaseous refrigerant, has low temperature, can be introduced into the outer jacket 4, and absorbs heat of tower top gas again under the swirling action of the swirling flow plate 5. The low-pressure gaseous refrigerant with the cold energy secondarily utilized is converged and flows out from the outlet of the outer jacket 4 and the outlet of the low-pressure gaseous refrigerant after flash evaporation on the third shell-side cylinder C3, and enters the absorber to continue the refrigeration cycle.
After the normal-temperature rich liquid in the inner heat exchange tube 2 absorbs heat, the normal-temperature rich liquid becomes a low-temperature rich liquid in a supercooled state, and then the solution pump is removed to continue the refrigeration cycle;
the tower top gas outside the outer heat exchange tube 3 is condensed into liquid after absorbing heat, one part is taken out as tower top product condensate, and the other part is taken as tower top reflux liquid to enter a rectifying tower for rectifying operation.
Example 3
As shown in fig. 6, the rectification system of this embodiment, on the basis of embodiment 2, includes a rectification tower and a reboiler, and further includes the above-mentioned composite condensation evaporator, for replacing the condenser in the existing rectification system, where the top gas of the rectification tower enters into the second shell side cylinder C2 of the composite condensation evaporator, exchanges heat with the medium in the outer heat exchange tube 3 and the outer jacket 4, and forms a top condensate, and a part of the top condensate is collected, and the other part is used as a top reflux liquid.
Example 4
As shown in fig. 6, the absorption refrigeration system of the present embodiment, on the basis of embodiment 2, includes an absorber, a solution pump, a generator, and a condenser, and the above-mentioned composite condensation evaporator, which is used for replacing the evaporator in the existing absorption refrigeration system, an expansion valve is disposed between the condenser and the composite condensation evaporator, and a high-pressure liquid refrigerant in the condenser forms a low-pressure gas-liquid saturated refrigerant through the expansion valve;
after the low-pressure gas-liquid saturated state refrigerant enters a third shell side cylinder C3 of the composite condensation evaporator, a part of the low-pressure gas-state refrigerant is flashed to form a low-pressure gas refrigerant to flow out from a first outlet of the low-pressure gas-state refrigerant, the other part of the flashed low-pressure liquid-state refrigerant downwards enters a cavity between the outer heat exchange tube 3 and the inner heat exchange tube 2, the heat of the tower top gas outside the outer heat exchange tube 3 and the normal-temperature rich liquid inside the inner heat exchange tube 2 is absorbed to be gasified into the low-pressure gas-state refrigerant, the low-pressure gas-state refrigerant is introduced into the outer jacket 4, the heat of the tower top gas is absorbed again under the swirling action of the swirling plate 5, the cold energy is converged with the low-pressure gas-state refrigerant flowing out from a second outlet of the low-pressure gas-state refrigerant after secondary use, and the low-pressure gas-state refrigerant flowing out from the first outlet of the low-pressure gas-state refrigerant is fed into the absorber, and the refrigerating circulation is continued;
the normal temperature rich liquid from the absorber enters the inner heat exchange tube 2, the normal temperature rich liquid in the inner heat exchange tube 2 is absorbed with heat and becomes the low temperature rich liquid in a supercooled state, and then the low temperature rich liquid is pumped into the generator by the solution pump to continue the refrigeration cycle.
Example 5
As shown in fig. 6, the absorption condensation rectification system in this embodiment includes the rectification system in embodiment 3 and the absorption refrigeration system in embodiment 4, the composite condensation evaporator in the rectification system and the composite condensation evaporator in the absorption refrigeration system are the same group, and the steam condensate outlet of the reboiler is connected to the heat source inlet of the generator, so that the steam condensate coming out from the reboiler of the rectification system is used as the heat source for driving the absorption refrigeration system.
The specific rectification refrigeration coupling process is as follows:
a rectifying tower, a reboiler and a pipeline of a composite condensation evaporator of the rectifying system are communicated, and a tower bottom gas-liquid circulation is established;
the method comprises the steps of (1) opening a heat source pipeline of a generator of an absorption refrigeration system, introducing a heat source discharged by a reboiler, heating, raising the temperature and the pressure of the generator, evaporating gaseous refrigerant in a working medium solution to generate the generator, condensing the gaseous refrigerant in the condenser, enabling the condensed high-pressure liquid refrigerant to pass through an expansion valve to obtain low-pressure gas-liquid saturated refrigerant, enabling the low-pressure gas-liquid saturated refrigerant to enter the composite condensation evaporator to exchange heat with the top gas of a rectifying tower, enabling the top gas to form a top condensate, enabling one part of the top gas to be collected, enabling the other part of the top gas to serve as top reflux liquid, establishing top gas-liquid circulation of the rectifying system, enabling the gas-liquid saturated refrigerant to evaporate to form gaseous refrigerant to enter the absorber, and enabling the solution of the absorber to be mixed and pumped into the generator through a solution, so as to establish refrigerant circulation.
In summary, the present invention focuses on that the low-pressure saturated refrigerant in the absorption refrigeration system for the composite condensation evaporator absorbs the heat of the top gas of the rectifying tower, and evaporates itself into a gaseous saturated refrigerant to enter the absorber, and the refrigeration cycle is continued. And the tower top gas is condensed into liquid after absorbing heat, one part is taken as tower top product condensate, and the other part is taken as tower top reflux liquid and enters a rectifying tower for rectifying operation. I.e. the composite condensation evaporator acts as a condenser in the rectification system and as an evaporator in the absorption refrigeration system.
And taking the steam condensate from the reboiler of the rectification system as a heat source for driving the absorption refrigeration system, namely introducing the steam condensate from the reboiler into a generator in the absorption refrigeration system, and preparing cold energy for a condenser in the rectification system by driving a thermodynamic working medium. The heat in the steam condensate discharged from the reboiler is recycled, so that the utilization rate of energy sources can be improved. Meanwhile, the cold energy produced by the refrigerating unit is used for cooling a condenser in the rectification system to replace the original circulating water, so that the consumption of the circulating water is reduced, and the energy consumption of public engineering is reduced. In addition, the temperature of the produced cold quantity is lower than that of the circulating water, so that the condensing pressure at the top of the rectifying tower can be reduced, the heat input at the bottom of the tower can be further reduced, and the energy consumption is reduced.
The vapor phase in the low-pressure state vapor-liquid saturated state refrigerant before entering the evaporator is separated, so that the evaporation efficiency can be greatly improved. And meanwhile, partial cold energy in the evaporator is used for cooling the normal-temperature rich liquid from the absorber to enable the normal-temperature rich liquid to be in a supercooled state, so that the normal-temperature rich liquid enters the solution pump, and cavitation of the solution pump can be avoided. The method replaces the original method (increases the height difference between the absorber and the solution pump), can reduce the cost of a unit pipeline, and simultaneously reduces the cost for ultra-high transportation.
The special design of the composite condensing evaporator structure embeds the absorption refrigeration system in the rectification system, and couples the rectification and refrigeration processes. Meanwhile, the special design of the composite condensation evaporator structure optimizes the refrigeration process internally, thereby further improving the refrigeration and rectification efficiency.
The foregoing examples illustrate only a few embodiments of the invention and are described in detail herein without thereby limiting the scope of the invention. It should be noted that it will be apparent to those skilled in the art that modifications can be made without departing from the spirit of the invention, which are within the scope of the invention.
Claims (9)
1. The composite condensing evaporator is characterized by comprising a cylinder body and sealing heads positioned at two ends of the cylinder body, wherein two outer tube plates and two inner tube plates are symmetrically arranged inside the cylinder body from outside to inside; a first shell-pass cylinder is arranged between one outer tube plate and the inner tube plate, a third shell-pass cylinder is arranged between the other outer tube plate and the inner tube plate, and a second shell-pass cylinder is arranged between the two inner tube plates;
a plurality of inner heat exchange tubes are uniformly distributed between the two outer tube plates, and two ends of each inner heat exchange tube are respectively communicated with sealing heads at two ends of the cylinder; a plurality of outer heat exchange tubes are uniformly distributed between the two inner tube plates, and two ends of each outer heat exchange tube are respectively communicated with the first shell side cylinder and the third shell side cylinder; the middle section of the inner heat exchange tube is positioned inside the outer heat exchange tube;
an outer jacket is arranged on the outer side of the second shell-side cylinder, and a group of swirl plates are welded and fixed between the outer jacket and the second shell-side cylinder;
one of the sealing heads is provided with a medium inlet, and the other sealing head is provided with a medium outlet; the third shell-side cylinder is provided with a low-pressure gas-liquid saturated medium inlet and a low-pressure gas medium first outlet, the first shell-side cylinder is provided with a low-pressure gas medium second outlet, the outer jacket is provided with a low-pressure gas medium inlet and a low-pressure gas medium second outlet at the head and the tail of the cyclone plate, and the second shell-side cylinder is provided with a gas inlet and a condensate outlet.
2. The composite condensation evaporator according to claim 1, wherein the low pressure gas-liquid saturated medium inlet is located at the upper side of the third shell side cylinder.
3. A composite condensation evaporator according to claim 1, wherein the composite condensation evaporator operates as follows:
the first medium circulates in the inner heat exchange tube, and the initial form of the first medium is normal-temperature medium; the third shell-side cylinder, the outer heat exchange tube, the first shell-side cylinder and the outer jacket are sequentially communicated with a second medium, and the initial form of the second medium is a low-pressure low-temperature gas-liquid saturated state; the second shell-side cylinder body circulates a third medium, and the initial form of the third medium is a high-temperature medium; the specific heat exchange process of the three media is as follows:
after the second medium in the low-pressure gas-liquid saturated state enters the third shell-pass cylinder, one part of the second medium is flashed to form a low-pressure gas medium which flows out from the first outlet of the low-pressure gas medium, the other part of the flashed low-pressure liquid medium downwards enters a cavity between the outer heat exchange tube and the inner heat exchange tube, absorbs the heat of the third medium outside the outer heat exchange tube and the heat of the first medium inside the inner heat exchange tube, is gasified into the low-pressure gas medium, is then introduced into the outer jacket, absorbs the heat of the third medium again under the swirling action of the swirling plate, and the low-pressure gas medium after secondary utilization flows out from the second outlet of the low-pressure gas medium and is merged with the low-pressure gas medium flowing out from the first outlet of the low-pressure gas medium to participate in the next flow;
after the first medium absorbs heat, the first medium becomes a supercooled medium and participates in the next process;
after the third medium absorbs heat, the third medium is condensed into a liquid state to participate in the next process.
4. A composite condensation evaporator according to claim 3, wherein the composite condensation evaporator operates as follows:
the first medium is normal-temperature rich liquid from the absorber, the second medium is low-pressure low-temperature gas-liquid saturated refrigerant which is from the condenser and passes through the expansion valve, and the third medium is tower top gas from the top of the rectifying tower;
after the low-pressure gas-liquid saturated refrigerant enters the third shell-side cylinder, part of the low-pressure gas-state refrigerant is flashed to form low-pressure gas-state refrigerant which flows out from the first outlet of the low-pressure gas-state refrigerant, and the other part of the flashed low-pressure liquid-state refrigerant downwards enters a cavity between the outer heat exchange tube and the inner heat exchange tube; the tower top gas from the rectifying tower enters a second shell-side cylinder from a gas inlet, and the normal-temperature rich liquid from the absorber enters an inner heat exchange tube;
the low-pressure liquid refrigerant after flash evaporation downwards enters a cavity between the outer heat exchange tube and the inner heat exchange tube, absorbs heat of tower top gas outside the outer heat exchange tube and normal-temperature rich liquid inside the inner heat exchange tube, is gasified into low-pressure gaseous refrigerant, is then introduced into an outer jacket, absorbs heat of the tower top gas again under the swirling action of a swirling plate, and cold energy is converged with the low-pressure gaseous refrigerant flowing out of a first outlet of the low-pressure gaseous refrigerant from a second outlet of the low-pressure gaseous refrigerant after secondary utilization, and enters an absorber to continue refrigeration cycle;
after the normal-temperature rich liquid in the inner heat exchange tube is absorbed by heat, the normal-temperature rich liquid becomes a low-temperature rich liquid in a supercooled state, and then the solution pump is removed to continue the refrigeration cycle;
the tower top gas outside the outer heat exchange tube is condensed into liquid after absorbing heat, one part is taken as tower top product condensate liquid, and the other part is taken as tower top reflux liquid and enters the rectifying tower for rectifying operation.
5. The composite condensation evaporator according to claim 1, wherein a plurality of baffle plates are arranged on the outer side of the outer heat exchange tube.
6. A rectification system comprising a rectification column and a reboiler, and further comprising the composite condensation evaporator according to any one of claims 1-5, wherein the top gas of the rectification column enters into the second shell side cylinder of the composite condensation evaporator, exchanges heat with the medium in the outer heat exchange tube and the outer jacket to form a top condensate, and a part of the top condensate is collected and the other part is used as top reflux.
7. An absorption refrigeration system comprises an absorber, a solution pump, a generator and a condenser, and is characterized by further comprising the composite condensation evaporator according to any one of claims 1-5, wherein an expansion valve is arranged between the condenser and the composite condensation evaporator, and high-pressure liquid refrigerant in the condenser passes through the expansion valve to form low-pressure gas-liquid saturated refrigerant;
after the low-pressure gas saturated state refrigerant enters the third shell side cylinder of the composite condensation evaporator, part of the low-pressure gas refrigerant is flashed to form low-pressure gas refrigerant to flow out from the first outlet of the low-pressure gas refrigerant, the other part of the flashed low-pressure liquid refrigerant enters a cavity between the outer heat exchange tube and the inner heat exchange tube downwards, the heat of the tower top gas outside the outer heat exchange tube and the normal-temperature rich liquid inside the inner heat exchange tube is absorbed, the low-pressure gas refrigerant is gasified to be low-pressure gas refrigerant, the low-pressure gas refrigerant is introduced into an outer jacket, the heat of the tower top gas is absorbed again under the swirling action of a swirling plate, the cold energy is converged by the low-pressure gas refrigerant which flows out from the second outlet of the low-pressure gas refrigerant and flows out from the first outlet of the low-pressure gas refrigerant, and the low-pressure gas refrigerant flows into an absorber, and the refrigeration cycle is continued;
the normal temperature rich liquid from the absorber enters the inner heat exchange tube, the normal temperature rich liquid in the inner heat exchange tube is absorbed by heat and becomes the low temperature rich liquid in a supercooled state, and then the low temperature rich liquid is pumped into the generator by the solution pump to continue the refrigeration cycle.
8. An absorption condensation rectification system, which is characterized by comprising the rectification system as claimed in claim 6 and the absorption refrigeration system as claimed in claim 7, wherein the composite condensation evaporator in the rectification system and the composite condensation evaporator in the absorption refrigeration system are in the same group, and a steam condensate outlet of a reboiler is connected with a heat source inlet of a generator and is used for taking steam condensate coming out of the reboiler of the rectification system as a heat source for driving the absorption refrigeration system.
9. A rectification and refrigeration coupling process, characterized by utilizing the absorption condensation rectification system as claimed in claim 8, comprising the following steps:
a rectifying tower, a reboiler and a pipeline of a composite condensation evaporator of the rectifying system are communicated, and a tower bottom gas-liquid circulation is established;
the method comprises the steps of (1) opening a heat source pipeline of a generator of an absorption refrigeration system, introducing a heat source discharged by a reboiler, heating, raising the temperature and the pressure of the generator, evaporating gaseous refrigerant in a working medium solution to generate the generator, condensing the gaseous refrigerant in the condenser, enabling the condensed high-pressure liquid refrigerant to pass through an expansion valve to obtain low-pressure gas-liquid saturated refrigerant, enabling the low-pressure gas-liquid saturated refrigerant to enter the composite condensation evaporator to exchange heat with the top gas of a rectifying tower, enabling the top gas to form a top condensate, enabling one part of the top gas to be collected, enabling the other part of the top gas to serve as top reflux liquid, establishing top gas-liquid circulation of the rectifying system, enabling the gas-liquid saturated refrigerant to evaporate to form gaseous refrigerant to enter the absorber, and enabling the solution of the absorber to be mixed and pumped into the generator through the solution pump, so as to establish refrigerant circulation.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN117771892A (en) * | 2024-02-27 | 2024-03-29 | 安徽普泛能源技术有限公司 | System and coupling machine for thermally-driven carbon capture pressure boosting and refrigeration deep coupling |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101502721A (en) * | 2009-02-12 | 2009-08-12 | 南京工业大学 | Adsorption type heat pump rectification system |
| CN101614496A (en) * | 2009-06-29 | 2009-12-30 | 张家港市江南锅炉压力容器有限公司 | Heating medium double tube plate heat exchanger |
| CN103954151A (en) * | 2014-04-24 | 2014-07-30 | 刘亚兵 | Novel high-efficiency heat exchanger |
| CN204555762U (en) * | 2015-03-06 | 2015-08-12 | 沈阳汇博热能设备有限公司 | Double tubesheet spiral baffle heat exchanger |
| CN212395918U (en) * | 2020-03-13 | 2021-01-26 | 江苏双良节能环保工程技术有限公司 | Methanol recovery tower or methanol rectification tower waste heat utilization system |
| CN115615065A (en) * | 2022-12-05 | 2023-01-17 | 安徽普泛能源技术有限公司 | Equipment for recovering outlet gas of safety valve and purifying non-condensable gas and application of equipment |
-
2023
- 2023-11-24 CN CN202311581139.5A patent/CN117287872B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101502721A (en) * | 2009-02-12 | 2009-08-12 | 南京工业大学 | Adsorption type heat pump rectification system |
| CN101614496A (en) * | 2009-06-29 | 2009-12-30 | 张家港市江南锅炉压力容器有限公司 | Heating medium double tube plate heat exchanger |
| CN103954151A (en) * | 2014-04-24 | 2014-07-30 | 刘亚兵 | Novel high-efficiency heat exchanger |
| CN204555762U (en) * | 2015-03-06 | 2015-08-12 | 沈阳汇博热能设备有限公司 | Double tubesheet spiral baffle heat exchanger |
| CN212395918U (en) * | 2020-03-13 | 2021-01-26 | 江苏双良节能环保工程技术有限公司 | Methanol recovery tower or methanol rectification tower waste heat utilization system |
| CN115615065A (en) * | 2022-12-05 | 2023-01-17 | 安徽普泛能源技术有限公司 | Equipment for recovering outlet gas of safety valve and purifying non-condensable gas and application of equipment |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN117771892A (en) * | 2024-02-27 | 2024-03-29 | 安徽普泛能源技术有限公司 | System and coupling machine for thermally-driven carbon capture pressure boosting and refrigeration deep coupling |
| CN117771892B (en) * | 2024-02-27 | 2024-06-04 | 安徽普泛能源技术有限公司 | System and coupling machine for thermally-driven carbon capture pressure boosting and refrigeration deep coupling |
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