WO2009092280A1 - 吸收溶液循环系统及方法 - Google Patents

吸收溶液循环系统及方法 Download PDF

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Publication number
WO2009092280A1
WO2009092280A1 PCT/CN2009/000027 CN2009000027W WO2009092280A1 WO 2009092280 A1 WO2009092280 A1 WO 2009092280A1 CN 2009000027 W CN2009000027 W CN 2009000027W WO 2009092280 A1 WO2009092280 A1 WO 2009092280A1
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WO
WIPO (PCT)
Prior art keywords
absorption solution
absorption
crystallization
absorbent
solution
Prior art date
Application number
PCT/CN2009/000027
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English (en)
French (fr)
Inventor
Qingquan Su
Original Assignee
Qingquan Su
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Publication date
Application filed by Qingquan Su filed Critical Qingquan Su
Priority to CNA2009100023820A priority Critical patent/CN101482340A/zh
Priority to CN2009801022151A priority patent/CN101918771B/zh
Priority to PCT/CN2009/000027 priority patent/WO2009092280A1/zh
Publication of WO2009092280A1 publication Critical patent/WO2009092280A1/zh

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Classifications

    • 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
    • F25B2315/00—Sorption refrigeration cycles or details thereof
    • F25B2315/002—Generator absorber heat exchanger [GAX]
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A30/00—Adapting or protecting infrastructure or their operation
    • Y02A30/27—Relating to heating, ventilation or air conditioning [HVAC] technologies
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02B—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO BUILDINGS, e.g. HOUSING, HOUSE APPLIANCES OR RELATED END-USER APPLICATIONS
    • Y02B30/00—Energy efficient heating, ventilation or air conditioning [HVAC]
    • Y02B30/62—Absorption based systems

Definitions

  • the present invention relates to a cycle technology in the field of thermal energy engineering, and more particularly to an absorption solution circulation system and a circulation method for an absorption heat pump cycle. Background technique
  • the existing absorption heat pump circulation system uses the absorption solution to precipitate the vapor of the low-boiling component under certain conditions, and under the other conditions, it can strongly absorb the low-boiling component vapor.
  • the two-component solution is often used as the absorption solution in the absorption refrigerating machine. It is customary to say that the low-boiling component is the working medium, and the high-boiling component is the absorbent.
  • the two form a working medium pair, generally using a water-lithium bromide working medium pair. .
  • the existing absorption heat pump circulation system mainly comprises: a generator 101 with a heat exchanger 110 installed therein, a condenser 102 with a heat exchanger 120 built therein, an evaporator 103 with a heat exchanger 130 installed therein, and a built-in replacement
  • the absorber 104 of the heater 140 has an absorption solution pump as an auxiliary device, a throttle (not shown), and the like.
  • the generator 101 and the condenser 102 are connected by a vapor passage 109, and the evaporator 103 and the absorber 104 are connected by a vapor passage 108.
  • the absorbing solution is circulated between the generator 101 and the absorber 104 through the absorbing solution conduits 106 and 105.
  • the working process of the existing absorption heat pump cycle includes: (1) heating a generator having a certain concentration of lithium bromide solution from the absorber 104 by using a driving heat source (such as steam, hot water, combustion flue gas, etc.), The concentrated lithium bromide solution formed is circulated to the absorber 104 by evaporating the water in the lithium bromide solution. (2) The water vapor enters the condenser 102 through the vapor passage 109, and is condensed into the condensed water by the cooling medium in the heat exchanger 120.
  • a driving heat source such as steam, hot water, combustion flue gas, etc.
  • the condensed water enters the evaporator 103 through the condensed water pipe 107, absorbs the heat of the working medium in the heat exchanger 130 to become low-pressure water vapor, and the heat of the working medium in the heat exchanger 130 is absorbed and the temperature is lowered. Therefore, it becomes the external cooling output of the absorption heat pump circulation system.
  • the low-pressure steam described above enters the generator 104 through the vapor passage 108, is absorbed by the concentrated lithium bromide solution from the generator 101, and generates heat of absorption, while the concentration of the lithium bromide solution is lowered, and the heat of absorption is controlled by the heat exchanger 140.
  • the cooling medium in the middle is taken away, and the low concentration lithium bromide solution is circulated to the generator 101.
  • the above-mentioned existing heat pump circulation system can also provide heat to the outside through the absorber, thereby Become a heating system.
  • the higher the concentration of lithium bromide in the absorber the higher the temperature at which the heat is output to the outside, that is, the lower the concentration of lithium bromide in the generator, the temperature of the externally driven heat source required. That is, the lower the grade.
  • the temperature rise is increased by increasing the lithium bromide concentration of the absorber (absorber)
  • the concentration of lithium bromide in the generator must be increased.
  • the main object of the present invention is to overcome the problems existing in the existing absorption heat pump circulation system, and to provide an absorption solution circulation system and method, the technical problem to be solved is that the absorption solution can be realized in the absorption and absorption in the absorption heat pump cycle. Circulation between the devices, thereby increasing the grade and efficiency of the output heat output or heat output of the absorption heat pump cycle.
  • an absorption solution circulation system wherein the absorption solution is composed of an absorbent and a working medium, and the absorption solution circulation system comprises: a generator and an absorber.
  • the system further comprises:
  • An absorbent crystallizer for cooling the absorption solution from the generator and/or the absorption solution from the absorber to form a crystallization solution of the absorption solution and the absorption agent, and the crystallization solution is sent to the generator after the crystallization
  • the absorbent crystals or the absorption solution containing the absorbent crystals are delivered to the absorber.
  • the foregoing absorption solution circulation system further comprises: an absorption solution from the heat exchanger, the absorption solution for crystallization after absorption and/or absorption of the absorbent or the absorption solution containing the absorption of the absorbent, and the absorption solution from the generator And/or an absorption solution from the absorber for heat exchange.
  • the foregoing absorption solution circulation system further comprises: an absorption solution from the heat exchanger for exchanging heat between the absorption solution from the absorber and the post-crystallization absorption solution from the absorbent crystallizer.
  • the foregoing absorption solution circulation system further comprises: an absorption solution from the heat exchanger, It is used to exchange the absorption solution from the absorber with the absorption crystal of the absorbent from the absorbent crystallizer or the absorption solution containing the absorption of the absorbent.
  • the foregoing absorption solution circulation system further comprises: an absorption solution from the heat exchanger for crystallizing or absorbing the absorption solution from the absorber with the crystallization solution and the absorbent from the absorbent crystallizer.
  • the absorption solution is subjected to heat exchange.
  • the aforementioned absorption solution circulation system the absorption solution from the generator and the absorption solution from the absorber are mixed into the absorption solution from the heat exchanger, and the absorption solution and the absorbent from the absorbent crystallizer are crystallized or contain an absorbent.
  • the crystallized absorption solution undergoes heat exchange.
  • an absorption solution circulation method wherein the absorption solution is composed of an absorbent and a working substance, and the method comprises the following steps: in the generator, heating the absorption solution to form a working fluid vapor and a first absorption solution Transferring the first absorption solution to the absorber; the absorption solution entering the absorber absorbs the working fluid vapor to form a second absorption solution; cooling the second absorption solution to form an absorption agent crystal and crystallization and absorbing the solution; The absorbent crystals or the absorption solution containing the absorbent crystals are sent to an absorber, and the post-crystallization absorption solution is sent to a generator.
  • the foregoing absorption solution circulation method further includes: the second absorption solution and the crystallization before the crystallization solution is transported to the generator after the crystallization, and before the second absorption solution is cooled. The solution is then absorbed for heat exchange.
  • the foregoing method for circulating the absorption solution further comprises: absorbing the crystallization of the absorbent or absorbing the crystal of the absorbent before the crystallization of the absorbent is transported to the absorber, and before the second absorbing solution is cooled.
  • the solution exchanges heat with the second absorption solution.
  • the foregoing method for circulating the absorption solution further comprises: before the crystallization solution is transported to the generator after the crystallization, the crystallization of the absorbent or the absorption solution containing the crystallization of the absorbent is delivered to the absorber, and the Before the second absorption solution is cooled, the second absorption solution exchanges heat with the post-crystallization absorption solution and the absorbent crystal or the absorption solution containing the absorption crystal.
  • the foregoing method for circulating the absorption solution further comprises: before the crystallization solution is transported to the generator after the crystallization, the crystallization of the absorbent or the absorption solution containing the crystallization of the absorbent is delivered to the absorber, the Before the second absorption solution is cooled, and before the first absorption solution is delivered to the absorber, the first absorption solution is mixed with the second absorption solution to form a mixture.
  • the absorption solution is heat-exchanged with the crystallization solution after absorption and the absorption crystallization of the absorbent or the absorption solution containing the crystallization of the absorbent.
  • the foregoing absorption solution circulation method wherein the working substance is one of water, methanol and ethanol or a mixture of several substances; the absorbent is LiBr, LiCK LiN0 3 , NaBr, KBr, CaCl 2 , MgBr A mixture of 2 and ZnCl 2 or a mixture of several substances.
  • the present invention has significant advantages and advantageous effects over the prior art. According to the above technical solution, since the absorption solution from the generator is cooled and crystallized and solid-liquid separated by using an absorbent crystallizer, a high concentration absorption solution and a low concentration absorption solution are formed, and are respectively used for the absorber and the occurrence.
  • the ability to reduce the quality of the generator's drive heat source while increasing the amount of heat that the absorber delivers outwards provides a technical way to convert lower grade waste heat into higher grade useful heat.
  • 1 is a flow chart of a conventional absorption heat pump circulation system.
  • Fig. 2 is a flow chart showing the first embodiment of the absorption solution circulation system of the present invention.
  • Fig. 3 is a flow chart showing the first embodiment of the absorption solution circulation system of the present invention.
  • Fig. 4 is a flow chart showing the third embodiment of the absorption solution circulation system of the present invention.
  • FIG. 5 is a flow chart showing Embodiment 4 of the absorption solution circulation system of the present invention.
  • Figure 6 is a flow chart showing the fifth embodiment of the absorption solution circulation system of the present invention.
  • Figure 7 is a flow chart showing the application of the absorption solution circulation system of the present invention to an absorption heat pump cycle.
  • the absorption solution circulation system includes: a generator 10, an absorber 20, and an absorbent crystallizer 40.
  • the generator 10 is configured to perform evaporation concentration on the absorption solution, that is, input a low concentration absorption solution, and simultaneously output the working medium vapor and the high concentration absorption solution.
  • the generator 10 has a working fluid vapor output pipe 11, an absorption solution input pipe 13 and an absorption solution output pipe 12.
  • the concentration of the absorption solution input into the absorption solution input pipe 13 is low.
  • After entering the generator 10, it is heated by an external heat source (not shown) to generate a working medium vapor, which is discharged from the working medium vapor output pipe 11 to cause the occurrence
  • the concentration of the absorbing solution in the device 10 is increased.
  • a high concentration of the absorption solution is output from the absorption solution output pipe 12.
  • the absorption solution input and absorption solution output of the generator 10 are continuously performed.
  • the absorber 20 is configured to absorb a working vapor by a high concentration of the absorption solution and release the heat of absorption.
  • the absorber 20 has a working fluid vapor inlet pipe 21, an absorption solution input pipe 23, and an absorption solution output pipe 22.
  • the concentration of the absorption solution input into the absorption solution input pipe 23 is higher than the concentration of the absorption solution of the output of the absorption solution output pipe 22.
  • the working fluid vapor entering the absorber 20 is absorbed by the high concentration absorption solution to release the absorption heat, which is output by the heat output device (not shown), and the concentration of the absorption solution is lowered, and the absorption solution after the concentration is lowered is
  • the absorption solution output pipe 22 is output.
  • the absorption solution input and absorption solution output of the absorber 20 are continuously performed.
  • An absorbent crystallizer 40 for cooling at least one of the absorbing solution from the generator 10 and the absorbing solution from the absorber 20 to cause the absorbing solution entering the absorbing agent crystallizer 40 to generate absorbing agent crystals, and
  • the crystallization of the absorbent is subjected to solid-liquid separation to form a crystallization solution of the absorbing solution and the absorbing agent.
  • the crystallization solution and the absorbent crystals are separately output after the crystallization.
  • the absorbing solution is sent to the generator 10 through the absorption solution input pipe 13, and the absorbing agent crystals or the absorbing solution containing the absorbing agent crystals are sent to the absorber 20 through the absorbing solution input pipe 23.
  • the absorbent crystallizer 40 cools the absorption solution with a refrigerant such as cold water or the like.
  • the absorbent crystallizer 40 further includes a refrigerant input conduit 41 and a refrigerant output conduit 42.
  • the absorbent crystallizer 40 may be configured by a combination of a cooling crystallization device and a solid-liquid separation device, or may perform simultaneous cooling crystallization and solid-liquid separation in one device, which is not limited in the present invention, and can achieve absorption.
  • a device for performing cooling crystallization and solid-liquid separation of the solution can be used in the present invention.
  • the absorption solution output line 12 of the generator 10 can be connected to the absorption solution input line of the absorber, whereby the absorption solution output from the generator 10 is crystallized and mixed with the absorbent and then input into the absorber.
  • the absorption solution circulation system constructed as described above can form a circulation of the absorption solution between the generator 10 and the absorber 20, and at the same time achieve the effect of outputting the working fluid vapor entering the absorber 20 via the generator 10, thereby achieving material balance.
  • the absorbent crystals described in this example and in the following examples are not intended to limit them to only absorbent crystal particles, but also include an absorbent solution containing absorbent crystal particles.
  • the absorption solution circulation system of the following embodiment further includes an absorption solution from the heat exchanger 30 for absorbing the solution from the generator and/or the absorption solution from the absorber with the absorber from the absorber, as compared to Example 1.
  • the absorption solution and/or the absorbing agent crystallize for heat exchange, increasing the temperature of the absorption solution entering the generator and/or the absorption solution entering the absorber, while reducing the temperature of the absorption solution entering the absorbent crystallizer, which is advantageous for saving
  • the amount of heat from the external cold source and the heat from the external heat source of the generator increase the amount of external heat output in the absorber.
  • the absorption solution circulation system of the present embodiment further includes an absorption solution from the heat exchanger 30 for changing the absorption solution from the absorber 20 and the post-crystallization absorption solution output from the absorbent crystallizer 40, as compared with the embodiment 1. heat.
  • the absorption solution output pipe 12 of the generator 10 is connected to the absorption solution input pipe of the absorber, whereby the absorption solution output from the generator 10 is crystallized and mixed with the absorbent and then input into the absorber.
  • the heat-absorbed absorption solution from the absorber is input to the absorbent crystallizer for cooling crystallization and solid-liquid separation; the crystallization-receiving solution output from the absorbent crystallizer 40 after heat exchange is sent to the generator 10. . Since the temperature of the absorbing solution from the absorber 20 is much higher than the temperature of the absorbing solution after crystallization from the absorbent crystallizer 40, the temperature of the absorbing solution entering the absorbent crystallizer 40 is greatly lowered after heat exchange, thereby being reduced The amount of cold used to cool the external source of the absorption solution. At the same time, the temperature of the absorbing solution after crystallization from the absorbent crystallizer after heat exchange is greatly increased, and it is sent to the generator. Compared with the first embodiment, the same working fluid vapor is evaporated. This embodiment can reduce the heat of the external heat source of the generator, thereby improving the energy utilization efficiency.
  • the absorption liquid circulation system of the present example further includes an absorption solution from the heat exchanger 30, It is used to exchange heat between the absorbing solution from the receiver 20 and the absorbing agent output from the absorbent crystallizer 40.
  • the absorption solution output pipe 12 of the generator 10 is connected to the absorption solution input pipe of the absorber, so that the absorption solution output from the generator 10 is crystallized and mixed with the heat-treated absorbent, and is input into the absorber.
  • the post-crystallization absorption solution output from the absorbent crystallizer 40 is sent to the generator 10 through the absorption solution input pipe 13.
  • the heat-absorbed absorption solution from the absorber 20 is input to the absorbent crystallizer 40 for cooling crystallization and solid-liquid separation; the heat-treated absorbent crystals output from the absorbent crystallizer 40 are passed through the absorption solution input pipe 23 It is delivered to the absorber 20. Since the temperature of the absorbing solution from the absorber 20 is much higher than the temperature at which the absorbing agent is output from the absorbing agent crystallizer 40, after the heat exchange, the absorption into the absorbing agent crystallizer 40 is simultaneously, after the heat transfer, the absorption is obtained. The temperature of the crystallization of the absorbent of the agent crystallizer is greatly increased, and it is transported to the absorber. Compared with the first embodiment, the same amount of working vapor is absorbed, and the heat of absorption can be released at a higher working temperature, thereby improving The temperature at which the absorber supplies heat to the outside increases the heating grade, thereby improving energy efficiency.
  • FIG. 5 is a flow chart of the absorption solution circulation system of Embodiment 4 of the present invention.
  • the crystallization solution output from the absorbent crystallizer 40 in this embodiment also passes the absorption solution from the absorber 20 and the absorption output from the absorbent crystallizer 40 from the heat exchanger 30 via the absorption solution. After the agent crystallizes and crystallizes, the solution is absorbed while heat exchange is performed. After the heat transfer, the absorption solution is sent to the generator 10 through the absorption solution input pipe 13.
  • the absorption solution output pipe 12 of the generator 10 is connected to the absorption solution input pipe of the absorber, so that the absorption solution output from the generator 10 is crystallized and mixed with the heat-treated absorbent, and is input into the absorber.
  • the post-crystallization absorption solution output from the absorbent crystallizer 40 is sent to the generator 10 through the absorption solution input pipe 13.
  • the heat-absorbed absorption solution from the absorber 20 is input to the absorbent crystallizer 40 for cooling crystallization and solid-liquid separation; the heat-treated absorbent crystals output from the absorbent crystallizer 40 are passed through the absorption solution input pipe 23 It is delivered to the absorber 20.
  • the temperature of the absorbing solution from the absorber 20 is much higher than the temperature of the absorbing agent crystallized from the absorbent crystallizer 40 and the absorbing solution after crystallization, the temperature of the absorbing solution entering the absorbent crystallizer 40 is greatly lowered after heat exchange. Thereby, the amount of cold of the external cold source for cooling the absorption solution can be reduced. At the same time, the temperature of the crystallization of the absorbent from the absorbent crystallizer after heat exchange is greatly increased, and it is sent to the absorber. Compared with the first embodiment, the same amount of working fluid vapor can be sucked, which can be higher. jobs The absorption heat is released at a temperature, thereby increasing the temperature at which the absorber is supplied to the outside and increasing the heating grade. After the heat exchange, the temperature of the crystallization solution from the absorbent crystallizer is greatly increased, and is sent to the generator to evaporate the same working fluid vapor. This embodiment can reduce the heat of the external heat source of the generator, thereby improving Energy efficiency.
  • Fig. 6 there is shown a flow chart of the absorption solution circulation system of the fifth embodiment of the present invention.
  • the absorption solution output line 12 of the generator 10 of the present embodiment is connected to the absorption solution absorption line 22 of the absorber 20, and the connected nodes are located before the absorption solution from the heat exchanger.
  • the absorbing solution from the generator 10 is mixed with the absorbing solution from the absorber 20 and then enters the absorbing solution from the heat exchanger 30, and the sorbent which is output from the absorbent crystallizer 40 is crystallized and crystallized to absorb the solution while heat exchange.
  • the absorption solution is sent to the generator 10 through the absorption solution input pipe 13; the heat-treated absorbent crystals are sent to the absorber 20 through the absorption solution input pipe 23.
  • the absorption solution from the generator 10 is mixed with the absorption solution from the absorber 20 to be cooled and crystallized, and the amount of the absorption solution cooled by crystallization is increased as compared with the foregoing embodiment, so that more crystallization solution after crystallization can be obtained. Thereby, the use efficiency of the absorbent crystallizer can be improved.
  • the working medium constituting the absorbing solution may be one of water, sterol and ethanol or a mixture of several substances; the absorbent is LiBr, LiC LiN0 3 , NaBr, KBr, CaCl 2 , MgBr 2 and One of ZnCl 2 or a mixture of several substances.
  • Embodiment 6 of the present invention also proposes an absorption solution circulation method which is carried out by using the absorption solution circulation system described in the above embodiment, the method comprising the following steps:
  • Part of the above second absorption solution is output to the absorber, and the output second absorption solution is cooled to generate absorbent crystals, which are separated by solid-liquid separation to form an absorbent crystal and a crystallization solution; the absorbent is crystallized and transported Into the absorber, the post-crystallization absorption solution is delivered to a generator.
  • the above various steps may be performed simultaneously, and the amount of working fluid vapor output from the generator is The amount of working fluid vapor supplied to the absorber is equal, thereby maintaining the material balance of the above-described absorption solution circulation process.
  • the first absorbing solution in this embodiment is an absorbing solution from the generator, and the second absorbing solution is an absorbing solution from the absorber.
  • the embodiment 7 of the present invention further provides an absorption solution circulation method, which, compared with the embodiment 6, further comprises: before the crystallization, the absorption solution is delivered to the generator, and the second absorption solution The step of exchanging heat between the second absorption solution and the post-crystallization absorption solution before cooling.
  • the embodiment 8 of the present invention further provides a method for circulating an absorption solution, which, in addition to the embodiment 6, further comprises: before the crystallization of the absorbent is transported to the absorber, and the second absorption solution is performed The crystallization of the absorbent is heat exchanged with the second absorbing solution prior to cooling.
  • the embodiment 9 of the present invention further provides an absorption solution circulation method, which, compared with the embodiment 6, further comprises: crystallization of the absorbent before the crystallization solution is transported to the generator after the crystallization Before the absorption to the absorber, and before the second absorption solution is cooled, the second absorption solution exchanges heat with the absorbent crystal after crystallization and absorption of the absorption solution.
  • the embodiment 10 of the present invention further provides an absorption solution circulation method.
  • the method further comprises: crystallization of the absorption agent before the crystallization solution is transported to the generator after the crystallization Before the second absorption solution is cooled before the second absorption solution is delivered to the absorber, and before the first absorption solution is delivered to the absorber, the first absorption solution is mixed with the second absorption solution to form a mixed absorption solution, the mixing The absorbing solution is condensed with the absorbent after crystallization and crystallization to absorb heat.
  • the working fluid is one of water, sterol and ethanol or a mixture of several substances;
  • the absorbent is LiBr, LiCl, LiN0 3 , NaBr, KBr, CaCl 2 , One of or a mixture of MgBr 2 and ZnCl 2 .
  • Fig. 7 there is shown a flow chart of an example of applying the absorption solution circulation system and method of the present invention to an absorption heat pump cycle for improving the energy grade of low temperature waste heat, and using lithium bromide and water to form an absorption solution.
  • the low temperature waste heat is used as an external heat source of the generator 10 and the evaporator 103, and the absorber 20 outputs the heat after the energy level is increased.
  • This example increases the low temperature residual heat of 10 (TC) to a saturated steam of 185 ° C.
  • This example uses Cooling water at 32 °C to cool the condenser and the absorbent crystallizer.
  • This example raises the low temperature residual heat at 75 °C to saturated steam at 150 °C.
  • This example uses 17 ° C of cooling water to cool the condenser and the absorbent crystallizer.
  • This example raises the low temperature residual heat at 90 °C to saturated steam at 170 °C.
  • This example uses 32 ° C cooling water to cool the condenser, while the cold compression generated by the vapor compression refrigeration cycle cools the absorbent crystallizer.
  • This comparative example uses the conventional absorption heat pump circulation system shown in Fig. 1 to raise the low-temperature residual heat at 100 °C to a saturated steam having a temperature of 150 °C.
  • the cooling water used in this comparative example was the same as in the above Example 1.
  • Table 1 below shows the operating parameters and performance of the above examples and comparative examples.
  • Imported lithium bromide concentration (wt%) 62. 5 60. 0 58. 0 62. 5
  • Lithium bromide concentration (wt%) 65. 5 63. 0 61. 0 65. 5 Pressure (kPa) 6. 1 2. 4 6. 1 6. 1 Heat exchanger inlet refrigerant temperature (.C) 32 15 32 32 Condensation
  • Imported lithium bromide concentration 75. 0 75. 0 75. 0 65. 5
  • Ethyl bromide concentration 72. 0 72. 0 72. 0 62. 5 Pressure (kPa) 82. 3 29. 9 55. 9 82. 3 Absorption
  • Agent junction lithium bromide crystallization temperature ( °C ) 37 19 4 - The above is only a preferred embodiment of the present invention, and is not intended to limit the scope of the present invention.
  • the present invention has been disclosed in the above preferred embodiments, it is not intended to limit the present invention.
  • the skilled person can make some modifications or modifications to the equivalent embodiments by using the above-disclosed technical contents without departing from the technical scope of the present invention, but without departing from the technical solution of the present invention, according to the present invention.
  • Technical simplifications Any simple modifications, equivalent changes and modifications made to the above embodiments are still within the scope of the technical solutions of the present invention.
  • the absorption solution circulation system of the invention can be applied to the absorption heat pump cycle, because the absorption crystallizer is used for cooling crystallization and solid-liquid separation of the absorption solution from the generator, thereby forming a high concentration absorption solution and a low concentration absorption solution.
  • the absorption crystallizer is used for cooling crystallization and solid-liquid separation of the absorption solution from the generator, thereby forming a high concentration absorption solution and a low concentration absorption solution.
  • absorbers and generators respectively, can reduce the requirements of the generator to drive the heat source grade, and at the same time increase the grade of heat transfer from the absorber, thus providing a way to convert lower grade waste heat into higher grades.
  • the technical approach to useful heat can be applied to the absorption heat pump cycle, because the absorption crystallizer is used for cooling crystallization and solid-liquid separation of the absorption solution from the generator, thereby forming a high concentration absorption solution and a low concentration absorption solution.

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Description

吸收溶液循环系统及方法 技术领域
本发明涉及一种热能工程领域的循环技术， 特别涉及一种用于吸收式 热泵循环的吸收溶液循环系统以及循环方法。 背景技术
请参阅图 1 所示， 现有的吸收式热泵循环系统， 利用吸收溶液在一定 条件下能析出低沸点组分的蒸气， 在另一条件下又能强烈地吸收低沸点组 分蒸气这一特性完成热泵循环。 目前吸收式制冷机中多采用二组分溶液作 为吸收溶液，习惯上称低沸点组分为工质， 高沸点组分为吸收剂， 二者组成 工质对，一般采用水-溴化锂工质对。 现有的吸收式热泵循环系统主要包括： 内设换热器 11 0的发生器 101、 内设换热器 120的冷凝器 102、 内设换热器 1 30的蒸发器 1 03和内设换热器 140的吸收器 104 , 另外还有作为辅助设备 的吸收溶液泵以及节流器（图中未示）等。 发生器 101和冷凝器 102通过 蒸气通路 109相连， 蒸发器 103和吸收器 104通过蒸气通路 108相连。 吸 收溶液通过吸收溶液管道 106和 105在发生器 101和吸收器 104之间进行 循环。
现有的吸收式热泵循环的工作过程包括： （1 )利用驱动热源（如蒸汽、 热水及燃烧烟气等）在发生器 101 中加热从吸收器 104输送来的具有一定 浓度的溴化锂溶液， 以使溴化锂溶液中的水蒸发出来， 形成的浓溴化锂溶 液循环到吸收器 104中。 （ 2 )水蒸气通过蒸气通路 109进入冷凝器 102中， 又被换热器 120 中的冷却工质冷凝成冷凝水。 （3 )该冷凝水经冷凝水管道 1 07进入蒸发器 1 03中， 吸收换热器 130中工质的热量而成为低压水蒸气， 换热器 130 中的工质的热量被吸收后温度降低， 从而成为该吸收式热泵循 环系统对外输出的冷量。 （4 )上述的低压水蒸气通过蒸气通路 108进入发 生器 104 ,被来自发生器 101中的浓溴化锂溶液吸收并产生吸收热， 同时溴 化锂溶液的浓度降低， 所述的吸收热由换热器 140 中的冷却工质带走， 低 浓度的溴化锂溶液循环至发生器 101中。
上述的现有的热泵循环系统也可以通过吸收器向外提供热量， 从而构 成供热系统。
对于吸收式热泵循环， 吸收器的溴化锂浓度越高， 则其向外输出热量 的温度即品位就越高， 在另一方面， 发生器的溴化锂浓度越低， 则其所需 外部驱动热源的温度即品位就越低。 可是， 以上所述的现有的吸收式热泵 循环系统， 由于其吸收器的溴化锂浓度总是低于其发生器的溴化锂浓度， 所以当通过提高其吸收器的溴化锂浓度以提高温升 （吸收器的吸收温度和 蒸发器的蒸发温度之差）或向外输出热量的品位时， 必定造成其发生器溴 化锂浓度的增大。 而为了实现在发生器 101 对高浓度的溴化锂溶液进行浓 缩， 就必须通过换热器 110对溴化锂溶液投入高品位的外部驱动热源， 这 不仅限制了其性能系数和温升的提高， 还限制了低温余热的有效利用。 发明内容
本发明的主要目的在于克服现有吸收式热泵循环系统存在的问题， 而 提供一种吸收溶液循环系统及方法，所要解决的技术问题是可以在吸收式 热泵循环中实现吸收溶液在发生器和吸收器之间的循环， 从而提高吸收式 热泵循环向外输出冷量或者热量的品位和效率。
本发明的目的及解决其技术问题是采用以下技术方案来实现的。 依据 本发明提出的一种吸收溶液循环系统， 所述的吸收溶液由吸收剂和工质组 成， 该吸收溶液循环系统包括： 发生器和吸收器 该系统还包括：
吸收剂结晶器， 用于对来自发生器的吸收溶液和 /或来自吸收器的吸收 溶液进行冷却， 形成结晶后吸收溶液和吸收剂结晶， 所述的结晶后吸收溶 液被输送至发生器， 所述的吸收剂结晶或者含吸收剂结晶的吸收溶液被输 送至吸收器。
本发明的目的及解决其技术问题还可采用以下技术措施进一步实现。 优选的， 前述的吸收溶液循环系统还包括： 吸收溶液自换热器， 用于 所述的结晶后吸收溶液和 /或吸收剂结晶或者含吸收剂结晶的吸收溶液，与 来自发生器的吸收溶液和 /或来自吸收器的吸收溶液进行换热。
优选的， 前述的吸收溶液循环系统， 其还包括： 吸收溶液自换热器， 用于将来自吸收器的吸收溶液与来自吸收剂结晶器的结晶后吸收溶液进行 换热。
优选的， 前述的吸收溶液循环系统， 其还包括： 吸收溶液自换热器， 用于将来自吸收器的吸收溶液与来自吸收剂结晶器的吸收剂结晶或者含吸 收剂结晶的吸收溶液进行换热。
优选的， 前述的吸收溶液循环系统， 其还包括： 吸收溶液自换热器， 用于将来自吸收器的吸收溶液与来自吸收剂结晶器的结晶后吸收溶液和吸 收剂结晶或者含吸收剂结晶的吸收溶液进行换热。
优选的， 前述的吸收溶液循环系统， 来自发生器的吸收溶液和来自吸 收器的吸收溶液混合后进入吸收溶液自换热器， 与来自吸收剂结晶器的吸 收溶液和吸收剂结晶或者含吸收剂结晶的吸收溶液进行换热。
本发明的目的及解决其技术问题是采用以下技术方案来实现的。 依据 本发明提出的一种吸收溶液循环方法， 所述的吸收溶液由吸收剂和工质组 成， 该方法包括以下步骤： 在发生器中， 对吸收溶液进行加热形成工质蒸 气和第一吸收溶液； 将第一吸收溶液输送到吸收器中； 进入吸收器的吸收 溶液吸收工质蒸气形成第二吸收溶液； 对所述第二吸收溶液进行冷却， 形 成吸收剂结晶和结晶后吸收溶液； 将所述的吸收剂结晶或者含吸收剂结晶 的吸收溶液输送到吸收器中， 将所述的结晶后吸收溶液输送到发生器中。
本发明的目的及解决其技术问题还可采用以下技术措施进一步实现。 优选的， 前述的吸收溶液循环方法， 还包括： 在所述的结晶后吸收溶 液输送到发生器之前， 且所述第二吸收溶液进行冷却之前， 所述的第二吸 收溶液与所述的结晶后吸收溶液进行换热。
优选的， 前述的吸收溶液循环方法， 还包括： 在所述的吸收剂结晶输 送到吸收器之前， 且所述第二吸收溶液进行冷却之前， 所述的吸收剂结晶 或者含吸收剂结晶的吸收溶液与所述的第二吸收溶液进行换热。
优选的， 前述的吸收溶液循环方法， 还包括： 在所述的结晶后吸收溶 液输送到发生器之前， 所述的吸收剂结晶或者含吸收剂结晶的吸收溶液输 送到吸收器之前， 且所述第二吸收溶液进行冷却之前， 所述第二吸收溶液 与结晶后吸收溶液和吸收剂结晶或者含吸收剂结晶的吸收溶液进行换热。
优选的， 前述的吸收溶液循环方法， 还包括： 在所述的结晶后吸收溶 液输送到发生器之前， 所述的吸收剂结晶或者含吸收剂结晶的吸收溶液输 送到吸收器之前， 所述第二吸收溶液进行冷却之前， 且所述第一吸收溶液 输送到吸收器之前， 所述第一吸收溶液与所述第二吸收溶液混合形成混合 吸收溶液， 该混合吸收溶液与结晶后吸收溶液和吸收剂结晶或者含吸收剂 结晶的吸收溶液进行换热。
优选的， 前述的吸收溶液循环方法， 其中所述工质为水、 甲醇和乙醇 其中之一或几种物质的混合物；所述吸收剂为 LiBr、 LiCK LiN03、 NaBr、 KBr、 CaCl2、 MgBr2 和 ZnCl2其中之一或几种物质的混合物。
本发明与现有技术相比具有明显的优点和有益效果。 由以上技术方案 可知，由于采用了吸收剂结晶器对来自发生器的吸收溶液进行冷却结晶及 固液分离， 从而形成高浓度的吸收溶液和低浓度的吸收溶液， 并分别用于 吸收器和发生器， 可以降低对发生器驱动热源品位的要求， 同时提高吸收 器向外输送热量的品位， 从而提供了一种可将更低品位的余热转化为更高 品位的有用热量的技术途径。
上述说明仅是本发明技术方案的概述， 为了能够更清楚了解本发明的 技术手段， 并可依照说明书的内容予以实施， 以下以本发明的较佳实施例 并配合附图详细说明如后。 附图说明
图 1是现有的吸收式热泵循环系统的流程图。
图 2是本发明的吸收溶液循环系统实施例 1的流程图。
图 3是本发明的吸收溶液循环系统实施例 1的流程图。
图 4是本发明的吸收溶液循环系统实施例 3的流程图。
图 5是本发明的吸收溶液循环系统实施例 4的流程图。
图 6是本发明的吸收溶液循环系统实施例 5的流程图。
图 7是将本发明的吸收溶液循环系统应用于吸收式热泵循环的 的流程图。
1 01： 发生器 102: 冷凝器
103: 蒸发器 104: 吸收器
107 : 冷凝水管道 108、 109: 蒸气通路
110、 120、 130、 140:换热器 实现发明的最佳方式
为更进一步阐述本发明为达成预定发明目的所采取的技术手段及功 效，以下结合附图及较佳实施例， 对依据本发明提出的吸收式热泵系统其具 体实施方式、 结构、 特征及其功效， 详细说明如后。
请参阅图 2所示，是本发明实施例 1的吸收溶液循环系统的流程图。 所 述的吸收溶液由吸收剂和工质组成， 本实施例中采用水 -溴化锂工质对作为 吸收溶液。 该吸收溶液循环系统包括： 发生器 1 0、 吸收器 20和吸收剂结晶 器 40。
所述的发生器 10 , 用于对吸收溶液进行蒸发浓缩， 即输入低浓度的吸 收溶液， 同时输出工质蒸气和高浓度的吸收溶液。 该发生器 1 0具有工质蒸 气输出管道 11、 吸收溶液输入管道 1 3和吸收溶液输出管道 12。 吸收溶液 输入管道 1 3输入的吸收溶液浓度较低，进入发生器 1 0之后被外部热源（图 中未示）加热产生工质蒸气， 该蒸气由工质蒸气输出管道 1 1排出， 从而使 发生器 10内的吸收溶液浓度提高。 高浓度的吸收溶液从吸收溶液输出管道 12输出。 发生器 10的吸收溶液输入和吸收溶液输出是连续进行的。
所述的吸收器 20 ,用于高浓度的吸收溶液吸收工质蒸气并释放吸收热。 该吸收器 20具有工质蒸气输入管道 21、 吸收溶液输入管道 23和吸收溶液 输出管道 22。吸收溶液输入管道 23输入的吸收溶液浓度高于吸收溶液输出 管道 22输出系吸收溶液的浓度。 进入吸收器 20的工质蒸气被高浓度的吸 收溶液所吸收释放出吸收热， 该吸收热被热量输出设备（图中未示）输出， 同时吸收溶液的浓度降低， 浓度降低后的吸收溶液由吸收溶液输出管道 22 输出。 吸收器 20的吸收溶液输入和吸收溶液输出是连续进行的。
吸收剂结晶器 40，用于至少对来自发生器 1 0的吸收溶液和来自吸收器 20的吸收溶液的其中之一进行冷却，使进入该吸收剂结晶器 40的吸收溶液 产生吸收剂结晶， 并对吸收剂结晶进行固液分离， 形成结晶后吸收溶液和 吸收剂结晶。 该结晶后吸收溶液和吸收剂结晶被分别输出。 结晶后吸收溶 液经吸收溶液输入管道 13输送到发生器 10中， 吸收剂结晶或者含吸收剂 结晶的吸收溶液经吸收溶液输入管道 23输送到吸收器 20中。 该吸收剂结 晶器 40采用冷媒 (例如冷水等）对吸收溶液进行冷却。 该吸收剂结晶器 40 还包括冷媒输入管道 41和冷媒输出管道 42。 该吸收剂结晶器 40可以采用 冷却结晶装置和固液分离装置相结合的方式构成， 也可以采用在一个装置 中同时进行冷却结晶和固液分离， 本发明对此不做限制， 能够实现对吸收 溶液进行冷却结晶和固液分离的装置皆可用于本发明中。 发生器 10的吸收 溶液输出管道 12可以与吸收器的吸收溶液输入管道相连，从而将发生器 10 输出的吸收溶液与所述的吸收剂结晶混合后共同输入到吸收器中。
如上述结构构成的吸收溶液循环系统， 可以形成吸收溶液在发生器 10 和吸收器 20之间的循环， 同时实现将进入吸收器 20的工质蒸气经由发生 器 10输出的效果， 从而达到物质平衡。 本实施例以及下述实施例中所述的 吸收剂结晶不用于限定其仅仅为吸收剂结晶颗粒， 其还包括含有吸收剂结 晶颗粒的吸收溶液。
与实施例 1相比， 下述实施例的吸收溶液循环系统还包括吸收溶液自 换热器 30,用于对来自发生器的吸收溶液和 /或来自吸收器的吸收溶液与来 自吸收剂结晶器的结晶后吸收溶液和 /或吸收剂结晶进行换热， 提高进入发 生器的吸收溶液和 /或进入吸收器的吸收溶液的温度， 同时降低进入吸收剂 结晶器的吸收溶液的温度， 有利于节约外部冷源的冷量和发生器的外部热 源的热量， 提高吸收器中对外的热量输出量。
请参阅图 3所示， 是本发明实施例 2吸收溶液循环系统的流程图。 与 实施例 1相比，本实施例的吸收溶液循环系统还包括吸收溶液自换热器 30， 用于使来自吸收器 20的吸收溶液与从吸收剂结晶器 40输出的结晶后吸收 溶液进行换热。 发生器 10的吸收溶液输出管道 12与吸收器的吸收溶液输 入管道相连， 从而将发生器 10输出的吸收溶液与所述的吸收剂结晶混合后 共同输入到吸收器中。 经过换热后的来自吸收器的吸收溶液输入到吸收剂 结晶器中进行冷却结晶和固液分离； 经过换热后的从吸收剂结晶器 40输出 的结晶后吸收溶液被输送至发生器 10中。 由于来自吸收器 20的吸收溶液 的温度远高于从吸收剂结晶器 40输出的结晶后吸收溶液的温度， 所以经过 换热后， 进入吸收剂结晶器 40的吸收溶液温度大大降低， 从而可以减少用 于冷却吸收溶液的外部冷源的冷量。 同时， 经过换热后的来自吸收剂结晶 器的结晶后吸收溶液的温度大大提高， 其被输送到发生器中。 与实施例 1 相比， 蒸发出同样的工质蒸气， 本实施例可以减少发生器的外部热源的热 量， 从而提高能源利用效率。
请参阅图 4所示， 是本发明实施例 3的吸收溶液循环系统的流程图。 与实施例 1相比，本实例的吸收 ^液循环系统还包括吸收溶液自换热器 30 , 用于使来自 收器 20的吸收溶液与从吸收剂结晶器 40输出的吸收剂结晶 进行换热。 发生器 10的吸收溶液输出管道 12与吸收器的吸收溶液输入管 道相连， 从而将发生器 10输出的吸收溶液与经过换热后的吸收剂结晶混合 后共同输入到吸收器中。 从吸收剂结晶器 40输出的结晶后吸收溶液经吸收 溶液输入管道 13输送到发生器 10内。 经过换热后的来自吸收器 20的吸收 溶液输入到吸收剂结晶器 40中进行冷却结晶和固液分离； 经过换热后的从 吸收剂结晶器 40输出的吸收剂结晶经吸收溶液输入管道 23被输送至吸收 器 20中。 由于来自吸收器 20的吸收溶液的温度远高于从吸收剂结晶器 40 输出的吸收剂结晶的温度， 所以经过换热后， 进入吸收剂结晶器 40的吸收 同时， 经过换热后的来自吸收剂结晶器的吸收剂结晶的温度大大提高， 其 被输送到吸收器中， 与实施例 1相比， 吸收同样量的工质蒸气， 可以在更 高的工作温度下释放吸收热， 从而可以提高吸收器向外供热的温度， 提高 供热品位， 从而提高能源利用效率。
请参阅图 5所示， 是本发明实施例 4的吸收溶液循环系统的流程图。 与实施例 3相比， 本实施例将从吸收剂结晶器 40输出的结晶后溶液也经由 吸收溶液自换热器 30， 使来自吸收器 20的吸收溶液与从吸收剂结晶器 40 输出的吸收剂结晶和结晶后吸收溶液同时进行换热。 经过换热后的结晶后 吸收溶液通过吸收溶液输入管道 13输送至发生器 10中。 发生器 10的吸收 溶液输出管道 12与吸收器的吸收溶液输入管道相连， 从而将发生器 10输 出的吸收溶液与经过换热后的吸收剂结晶混合后共同输入到吸收器中。 从 吸收剂结晶器 40输出的结晶后吸收溶液经吸收溶液输入管道 13输送到发 生器 10 内。 经过换热后的来自吸收器 20的吸收溶液输入到吸收剂结晶器 40中进行冷却结晶和固液分离；经过换热后的从吸收剂结晶器 40输出的吸 收剂结晶经吸收溶液输入管道 23被输送至吸收器 20中。 由于来自吸收器 20的吸收溶液的温度远高于从吸收剂结晶器 40输出的吸收剂结晶和结晶后 吸收溶液的温度， 所以经过换热后， 进入吸收剂结晶器 40的吸收溶液温度 大大降低， 从而可以减少用于冷却吸收溶液的外部冷源的冷量。 同时， 经 过换热后的来自吸收剂结晶器的吸收剂结晶的温度大大提高， 其被输送到 吸收器中， 与实施例 1相比， 吸吹同样量的工质蒸气， 可以在更高的工作 温度下释放吸收热， 从而可以提高吸收器向外供热的温度， 提高供热品位。 经过换热后的来自吸收剂结晶器的结晶后溶液的温度大大提高， 其被输送 到发生器中， 蒸发出同样的工质蒸气， 本实施例可以减少发生器的外部热 源的热量， 从而提高能源利用效率。
请参阅图 6所示， 是本发明实施例 5的吸收溶液循环系统的流程图。 与实施例 4相比， 本实施例的发生器 10的吸收溶液输出管道 12与吸收器 20的吸收溶液吸收管道 22相连，相连的节点位于进入吸收溶液自换热器之 前。 来自发生器 10的吸收溶液与来自吸收器 20的吸收溶液混合后进入吸 收溶液自换热器 30,与从吸收剂结晶器 40输出的吸收剂结晶和结晶后吸收 溶液同时进行换热。 经过换热后的结晶后吸收溶液通过吸收溶液输入管道 13输送至发生器 10 中； 经过换热后的吸收剂结晶通过吸收溶液输入管道 23输送至吸收器 20中。将来自发生器 10的吸收溶液与来自吸收器 20的吸 收溶液混合后进行冷却结晶， 与前述实施例相比， 增加了被冷却结晶的吸 收溶液的量， 从而可以得到更多的结晶后吸收溶液， 从而可以提高吸收剂 结晶器的使用效率。
在上述实施例中， 组成吸收溶液的工质可以为水、 曱醇和乙醇其中之 一或几种物质的混合物； 所述吸收剂为 LiBr、 LiC LiN03、 NaBr、 KBr、 CaCl2、 MgBr2 和 ZnCl2其中之一或几种物质的混合物。
本发明的实施例 6还提出一种吸收溶液循环方法， 采用上述实施例所 述的吸收溶液循环系统进行， 该方法包括以下步骤：
对发生器中的吸收溶液进行加热形成工质蒸气和第一吸收溶液， 所述 工质蒸气通过管道输出发生器， 所述第一吸收溶液也通过管道输出发生器， 并被输送至吸收器中；
向吸收器提供工质蒸气， 在吸收器内该工质蒸气被吸收溶液所吸收形 成第二吸收溶液同时释放吸收热 , 该吸收热通过热量输出设备输出；
将部分上述的第二吸收溶液输出吸收器， 并对输出的第二吸收溶液进 行冷却产生吸收剂结晶， 经固液分离后形成吸收剂结晶和结晶后吸收溶液； 将所述的吸收剂结晶输送到吸收器中， 将所述的结晶后吸收溶液输送 到发生器中。
上述的各个步骤可以是同时进行的， 从发生器输出的工质蒸气的量与 向吸收器提供的工质蒸气的量相等， 从而使上述吸收溶液循环过程保持物 质平衡。
与上述实施例 1-5相对应， 本实施例中的第一吸收溶液是来自发生器 的吸收溶液， 第二吸收溶液是来自吸收器的吸收溶液。
较佳的， 本发明的实施例 7还提出一种吸收溶液循环方法， 与实施例 6 相比， 还包括： 在所述的结晶后吸收溶液输送到发生器之前， 且所述第二 吸收溶液进行冷却之前， 所述的第二吸收溶液与所述的结晶后吸收溶液进 行换热的步骤。
较佳的， 本发明的实施例 8还提出一种吸收溶液循环方法， 与实施例 6 相比， 还包括： 在所述的吸收剂结晶输送到吸收器之前， 且所述第二吸收 溶液进行冷却之前， 所述的吸收剂结晶与所述的第二吸收溶液进行换热。
较佳的， 本发明的实施例 9还提出一种吸收溶液循环方法， 与实施例 6 相比， 还包括： 在所述的结晶后吸收溶液输送到发生器之前， 所述的吸收 剂结晶输送到吸收器之前， 且所述第二吸收溶液进行冷却之前， 所述第二 吸收溶液与所述的吸收剂结晶和结晶后吸收溶液进行换热。
较佳的， 本发明的实施例 10还提出一种吸收溶液循环方法， 与实施例 6相比， 还包括： 在所述的结晶后吸收溶液输送到发生器之前， 所述的吸收 剂结晶在输送到吸收器之前， 所述第二吸收溶液进行冷却之前， 且所述第 一吸收溶液输送到吸收器之前， 所述第一吸收溶液与所述第二吸收溶液混 合形成混合吸收溶液 , 该混合吸收溶液与所述的吸收剂结晶和结晶后吸收 溶液进行换热。
在本发明提出的吸收溶液循环方法， 其中所述工质为水、 曱醇和乙醇 其中之一或几种物质的混合物；所述吸收剂为 LiBr、 LiCl、 LiN03、 NaBr、 KBr、 CaCl2、 MgBr2 和 ZnCl2其中之一或几种物质的混合物。
请参阅图 7 所示， 是将本发明的吸收溶液循环系统以及方法应用于吸 收式热泵循环的一个例子的流程图， 用于提高低温余热的能量品位， 并采 用溴化锂和水组成吸收溶液。 所述低温余热作为发生器 10和蒸发器 103的 外部热源， 吸收器 20输出能量品位提高后的热量。
实例 1
本实例将 10(TC的低温余热提升为温度 185。C的饱和蒸汽。 本实例使用 32 °C的冷却水来冷却冷凝器和吸收剂结晶器。
实例 2
本实例将 75 °C的低温余热提升为温度 150 °C的饱和蒸汽。 本实例使用 17 °C的冷却水来冷却冷凝器和吸收剂结晶器。
实例 3
本实例将 90 °C的低温余热提升为温度 170 °C的饱和蒸汽。 本实例使用 32 °C的冷却水来冷却冷凝器， 而采用蒸气压缩式制冷循环产生的冷量来冷 却吸收剂结晶器。
比较例
本比较例采用图 1所示的现有吸收式热泵循环系统，将 100 °C的低温余 热提升为温度 150°C的饱和蒸汽。本比较例使用的冷却水与上述实例 1相同。
下表 1为上述实例与比较例的工作参数和性能。
表 1
比较 实例 1 实例 2 实例 3
例 低温余热温度（ °C ) 100 75 90 100 低温余热的利用后温度（ °C ) 95 70 85 95 发生
进口溴化锂浓度 ( wt% ) 62. 5 60. 0 58. 0 62. 5 器
出口溴化锂浓度 ( wt% ) 65. 5 63. 0 61. 0 65. 5 压力 (kPa) 6. 1 2. 4 6. 1 6. 1 换热器进口冷媒温度（。C ) 32 15 32 32 冷凝
换热器出口冷媒温度（ Γ ) 35 18 35 35 器
压力 ( kPa ) 6. 0 2. 3 6. 0 6. 0 换热器进口低温余热温度（ °C ) 100 75 90 100 蒸发
哭 换热器出口低温余热温度、即低温余
95 70 85 95 热的利用后温度（。C )
压力 ( kPa ) 82. 4 30. 0 56. 0 82. 4 换热器入口冷凝水温度（ °C ) 100 75 90 100 换热器出口饱和蒸汽温度（。C ) 185 150 170 150 吸收
进口溴化锂浓度 ( wt% ) 75. 0 75. 0 75. 0 65. 5 器
出口溴化锂浓度 ( wt% ) 72. 0 72. 0 72. 0 62. 5 压力（kPa) 82. 3 29. 9 55. 9 82. 3 吸收
剂结 溴化锂晶析温度（ °C ) 37 19 4 - 以上所述， 仅是本发明的较佳实施例而已， 并非对本发明作任何形式 上的限制， 虽然本发明已以较佳实施例揭露如上， 然而并非用以限定本发 明，任何熟悉本专业的技术人员， 在不脱离本发明技术方案范围内，当可利 用上述揭示的技术内容作出些许更动或修饰为等同变化的等效实施例，但 凡是未脱离本发明技术方案的内容， 依据本发明的技术实质对以上实施例 所作的任何简单修改、 等同变化与修饰， 均仍属于本发明技术方案的范围 内。 工业应用性
本发明的吸收溶液循环系统可应用于吸收式热泵循环， 由于采用了吸 收剂结晶器对来自发生器的吸收溶液进行冷却结晶及固液分离， 从而形成 高浓度的吸收溶液和低浓度的吸收溶液， 并分别用于吸收器和发生器， 可 以降低对发生器驱动热源品位的要求， 同时提高吸收器向外输送热量的品 位， 从而提供了一种可将更低品位的余热转化为更高品位的有用热量的技 术途径。

Claims

权 利 要 求
1、 一种吸收溶液循环系统， 所述的吸收溶液由吸收剂和工质组成， 该 吸收溶液循环系统包括： 发生器和吸收器， 其特征在于， 该系统还包括： 吸收剂结晶器， 用于对来自发生器的吸收溶液和 /或来自吸收器的吸收 溶液进行冷却， 形成结晶后吸收溶液和吸收剂结晶， 所述的结晶后吸收溶 液被输送至发生器， 所述的吸收剂结晶或者含吸收剂结晶的吸收溶液被输 送至吸收器。
2、 根据权利要求 1所述的吸收溶液循环系统， 其特征在于， 该系统还 包括： 吸收溶液自换热器， 用于所述的结晶后吸收溶液和 /或吸收剂结晶或 者含吸收剂结晶的吸收溶液，与来自发生器的吸收溶液和 /或来自吸收器的 吸收溶液进行换热。
3、 根据权利要求 1所述的吸收溶液循环系统， 其特征在于其还包括： 吸收溶液自换热器， 用于将来自吸收器的吸收溶液与来自吸收剂结晶器的 结晶后吸收溶液进行换热。
4、 根据权利要求 1所述的吸收溶液循环系统， 其特征在于其还包括： 吸收溶液自换热器， 用于将来自吸收器的吸收溶液与来自吸收剂结晶器的 吸收剂结晶或者含吸收剂结晶的吸收溶液进行换热。
5、 根据权利要求 1所述的吸收溶液循环系统， 其特征在于其还包括： 吸收溶液自换热器， 用于将来自吸收器的吸收溶液与来自吸收剂结晶器的 结晶后吸收溶液和吸收剂结晶或者含吸收剂结晶的吸收溶液进行换热。
6、 根据权利要求 5所述的吸收溶液循环系统， 其特征在于来自发生器 的吸收溶液和来自吸收器的吸收溶液混合后进入吸收溶液自换热器， 与来 自吸收剂结晶器的吸收溶液和吸收剂结晶或者含吸收剂结晶的吸收溶液进 行换热。
7、 一种吸收溶液循环方法， 所述的吸收溶液由吸收剂和工质组成， 其 特征在于该方法包括以下步骤：
在发生器中， 对吸收溶液进行加热形成工质蒸气和第一吸收溶液； 将第一吸收溶液输送到吸收器中；
进入吸收器的吸收溶液吸收工质蒸气形成第二吸收溶液； 对所述第二吸收溶液进行冷却， 形成吸收剂结晶和结晶后吸收溶液； 将所述的吸收剂结晶或者含吸收剂结晶的吸收溶液输送到吸收器中， 将所述的结晶后吸收溶液输送到发生器中。
8、 根据权利要求 7所述的吸收溶液循环方法， 其特征在于还包括： 在所述的结晶后吸收溶液输送到发生器之前， 且所述第二吸收溶液进 行冷却之前， 所述的第二吸收溶液与所述的结晶后吸收溶液进行换热。
9、 根据权利要求 7所述的吸收溶液循环方法， 其特征在于还包括： 在所述的吸收剂结晶或者含吸收剂结晶的吸收溶液输送到吸收器之 前， 且所述第二吸收溶液进行冷却之前， 所述的吸收剂结晶或者含吸收剂 结晶的吸收溶液与所述的第二吸收溶液进行换热。
10、 根据权利要求 7所述的吸收溶液循环方法， 其特征在于还包括： 在所述的结晶后吸收溶液输送到发生器之前， 所述的吸收剂结晶或者 含吸收剂结晶的吸收溶液输送到吸收器之前， 且所述第二吸收溶液进行冷 却之前， 所述第二吸收溶液与所述的结晶后吸收溶液和吸收剂结晶或者含 吸收剂结晶的吸收溶液进行换热。
11、 根据权利要求 7所述的吸收溶液循环方法， 其特征在于还包括： 在所述的结晶后吸收溶液输送到发生器之前， 所述的吸收剂结晶或者 含吸收剂结晶的吸收溶液输送到吸收器之前， 所述第二吸收溶液进行冷却 之前， 且所述第一吸收溶液输送到吸收器之前， 所述第一吸收溶液与所述 第二吸收溶液混合形成混合吸收溶液， 该混合吸收溶液与所述的结晶后吸 收溶液和吸收剂结晶或者含吸收剂结晶的吸收溶液进行换热。
12、 根据权利要求 7所述的吸收溶液循环方法， 其特征在于， 其中所述工质为水、 曱醇和乙醇其中之一或几种物质的.混合物； 所述 吸收剂为 LiBr、 LiCl、 LiN03、 NaBr、 KBr、 CaCl2、 MgBr2 和 ZnCl2 其中之一或几种物质的混合物。
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