WO2018056024A1 - 吸収式冷凍機 - Google Patents

吸収式冷凍機 Download PDF

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Publication number
WO2018056024A1
WO2018056024A1 PCT/JP2017/031613 JP2017031613W WO2018056024A1 WO 2018056024 A1 WO2018056024 A1 WO 2018056024A1 JP 2017031613 W JP2017031613 W JP 2017031613W WO 2018056024 A1 WO2018056024 A1 WO 2018056024A1
Authority
WO
WIPO (PCT)
Prior art keywords
solution
pressure regenerator
regenerator
absorber
auxiliary
Prior art date
Application number
PCT/JP2017/031613
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English (en)
French (fr)
Japanese (ja)
Inventor
浩伸 川村
藤居　達郎
武田　伸之
Original Assignee
日立ジョンソンコントロールズ空調株式会社
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by 日立ジョンソンコントロールズ空調株式会社 filed Critical 日立ジョンソンコントロールズ空調株式会社
Priority to KR1020187009541A priority Critical patent/KR102017436B1/ko
Priority to CN201780003541.1A priority patent/CN108139126B/zh
Publication of WO2018056024A1 publication Critical patent/WO2018056024A1/ja

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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
    • F25B15/008—Sorption machines, plants or systems, operating continuously, e.g. absorption type with multi-stage operation
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B15/00—Sorption machines, plants or systems, operating continuously, e.g. absorption type
    • F25B15/02—Sorption machines, plants or systems, operating continuously, e.g. absorption type without inert gas
    • F25B15/06—Sorption machines, plants or systems, operating continuously, e.g. absorption type without inert gas the refrigerant being water vapour evaporated from a salt solution, e.g. lithium bromide
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B33/00—Boilers; Analysers; Rectifiers
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B41/00—Fluid-circulation arrangements
    • F25B41/40—Fluid line arrangements
    • 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 an absorption refrigerator.
  • the absorption refrigerator can be driven by heat
  • cold water can be supplied using hot water generated as exhaust heat as a driving heat source.
  • cold water of about 7 ° C. can be supplied using hot water of about 90 ° C. as a driving heat source.
  • Patent Document 1 describes that the regenerator is an absorption refrigerator having two two-stage absorption cycles, and cold water can be supplied using hot water having a temperature lower than that of an absorption refrigerator having a single effect cycle as a driving heat source. .
  • Patent Document 2 describes an absorption refrigerator that combines a single effect cycle and an auxiliary cycle (two-stage absorption cycle). This is a series flow in which a high-pressure regenerator and a low-pressure regenerator are provided on the single effect cycle side, and the entire amount of the solution is circulated in the order of the absorber, the high-pressure regenerator, the low-pressure regenerator, and the absorber.
  • the auxiliary cycle side is composed of an auxiliary absorber and an auxiliary regenerator.
  • the gas phase part of the auxiliary absorber communicates with the low pressure regenerator, and the gas phase part of the auxiliary regenerator is the gas phase part of the high pressure regenerator and the condenser.
  • the structure communicated with is described.
  • Patent Document 2 it is assumed that hot water of a driving heat source can be used from one temperature required for an absorption refrigerator of a single effect cycle to a temperature required for an absorption refrigerator of a two-stage absorption cycle in one absorption refrigerator.
  • hot water of about 90 ° C. is used as a driving heat source for an absorption refrigerator of a single effect cycle, and hot water whose temperature has subsequently decreased is used as a driving heat source of an absorption refrigerator of a two-stage absorption cycle.
  • two absorption refrigerators having different cycle configurations are required, and two piping systems for chilled water and cooling water are required, which complicates the piping configuration and increases the installation area and costs.
  • the number of solution pumps and refrigerant pumps almost doubles, increasing the amount of power consumption and also doubling the amount of solution and the amount of refrigerant.
  • An object of the present invention is to obtain an absorption refrigerator that can reduce the amount of solution retained in a configuration in which an auxiliary cycle is combined with a single effect cycle.
  • an absorption refrigerator includes an evaporator, an absorber, a low-pressure regenerator, a high-pressure regenerator, an auxiliary absorber, an auxiliary regenerator, and a condenser. And a solution pump.
  • the evaporator, the absorber, the low pressure regenerator, the high pressure regenerator, the auxiliary absorber, and the auxiliary regenerator are a falling liquid film type.
  • the vaporizer communicates with the evaporator and the absorber
  • the low-pressure regenerator and the auxiliary absorber communicate with the gas-phase portion
  • the regenerator and the condenser communicate with each other in a gas phase portion, and a solution pipe for flowing a solution from the high pressure regenerator to the absorber is connected to a solution pipe for flowing a solution from the low pressure regenerator.
  • the solution pump is provided in the solution pipe from the merge portion to the absorber, Bottom of the serial high-pressure regenerator is located higher than the bottom surface of the low-pressure regenerator.
  • an absorption chiller capable of reducing the amount of solution retained in a configuration in which an auxiliary cycle is combined with a two single effect cycle.
  • the cycle system diagram of the absorption refrigerating machine concerning the embodiment of the present invention is shown.
  • the dueling diagram of the absorption refrigerating machine concerning the embodiment of the present invention is shown.
  • FIG. 1 shows a cycle system diagram of the absorption refrigerator 100 of the present embodiment.
  • FIG. 2 shows a dueling diagram of the absorption refrigerator 100 of the present embodiment.
  • the horizontal axis indicates the solution temperature and the vertical axis indicates the pressure, and the state of the cycle of the present invention is shown in the During diagram composed of the isoconcentration lines of the solution.
  • the absorption refrigerator 100 includes a single effect cycle side and an auxiliary cycle (two-stage absorption cycle) side, and the solution circulates independently in each cycle.
  • the single effect cycle side includes an evaporator 1 (E), an absorber 9 (A), a low pressure regenerator 22 (LG), a high pressure regenerator 33 (HG), a condenser 40 (C), a low temperature solution heat exchanger 55, The heat exchanger element of the high temperature solution heat exchanger 56, the refrigerant pump 6, the solution pumps 14 and 30, and the like are provided.
  • the auxiliary cycle side includes an auxiliary absorber 16 (AA), an auxiliary regenerator 44 (AG), a heat exchanger element of an intermediate temperature solution heat exchanger 57, solution pumps 29 and 54, and the like.
  • the refrigerant stored in the lower part of the evaporator 1 by the refrigerant pump 6 is guided to the spraying device 2 through the refrigerant pipe 7 and sprayed outside the heat transfer tube of the heat exchanger 3.
  • the dispersed refrigerant is heated by the cold water flowing in the heat transfer pipe of the heat exchanger 3 to be partially refrigerant vapor, and is led to the absorber 9 through the eliminator 8.
  • the cold water flowing in the heat transfer tube of the heat exchanger 3 is cooled using the latent heat of vaporization when the refrigerant evaporates.
  • Cold water pipes 4 and 5 are connected to the heat exchanger 3 to pass cold water for supplying cold heat to the load side.
  • the solution concentrated by the low pressure regenerator 22 and the high pressure regenerator 33 is scattered from the spray device 10 to the outside of the heat transfer tube of the heat exchanger 11.
  • the dispersed solution absorbs the refrigerant vapor from the evaporator 1 and decreases in concentration, and then branches at the branch point A after passing through the low-temperature solution heat exchanger 55 by the solution pump 14 installed in the middle of the solution pipe 15.
  • One is led to the low pressure regenerator 22 through the flow rate adjustment valve 32 of the solution pipe 31.
  • the other solution branched at the branch point A is led to the high pressure regenerator 33 through the high temperature solution heat exchanger 56.
  • Cooling water is passed through the heat transfer tube of the heat exchanger 11 of the absorber 9 in order to remove the absorption heat generated when the solution absorbs the refrigerant vapor. Cooling water pipes 12 and 13 are connected to the heat exchanger 11.
  • the solution having a reduced concentration in the absorber 9 is sprayed from the spray device 23 to the outside of the heat transfer tube of the heat exchanger 24.
  • the dispersed solution is heated by a heat source medium flowing in the heat transfer tube of the heat exchanger 24 and separated into a concentrated solution and refrigerant vapor.
  • the concentrated solution merges with the solution from the high pressure regenerator 33 at the merge point (merging portion) B through the solution pipe 27.
  • the refrigerant vapor separated from the concentrated solution is guided to the auxiliary absorber 16 on the auxiliary cycle side via the eliminator 21.
  • Heat source medium pipes 25 and 26 are connected to the heat exchanger 24 of the low pressure regenerator 22.
  • the solution whose concentration is reduced by the absorber 9 and heated by the low-temperature solution heat exchanger 55 and the high-temperature solution heat exchanger 56 is sprayed from the spraying device 34 to the outside of the heat transfer tube of the heat exchanger 35.
  • the sprayed solution is heated by a heat source medium flowing in the heat transfer tube of the heat exchanger 35 and separated into a concentrated solution and refrigerant vapor.
  • the concentrated solution is guided to the junction B through a high temperature solution heat exchanger 56 installed in the middle of the solution pipe 49.
  • the concentrated solution from the low pressure regenerator 22 and the high pressure regenerator 33 that have joined at the junction B is boosted by the solution pump 30 and led to the absorber 9 through the low temperature solution heat exchanger 55.
  • the refrigerant vapor separated from the solution concentrated by the high pressure regenerator 33 is guided to the condenser 40 through the baffle 39.
  • Heat source medium pipes 36 and 37 are connected to the heat exchanger 35 of the high pressure regenerator 33.
  • the refrigerant vapor separated from the solution concentrated in the high pressure regenerator 33 and the auxiliary regenerator 44 is cooled with cooling water flowing in the heat transfer tube of the heat exchanger 41 to be condensed and liquefied.
  • the condensed and liquefied refrigerant is guided to the evaporator 1 through the refrigerant pipe 50.
  • Cooling water pipes 42 and 43 are connected to the heat exchanger 41.
  • the solution concentrated in the auxiliary regenerator 44 is sprayed from the spraying device 17 to the outside of the heat transfer tube of the heat exchanger 18.
  • the sprayed solution absorbs the refrigerant vapor from the low-pressure regenerator 22 of the single effect side cycle and becomes low in concentration, and then passes through the intermediate-temperature solution heat exchanger 57 with the solution pump 29 installed in the middle of the solution pipe 28 and then the high-pressure. Guided to the regenerator 33.
  • Cooling water is passed through the heat transfer tube of the heat exchanger 18 of the auxiliary absorber 16 in order to remove absorption heat generated when the solution absorbs the refrigerant vapor. Cooling water pipes 19 and 20 are connected to the heat exchanger 18.
  • the solution whose concentration has been reduced by the auxiliary absorber 16 is sprayed from the spraying device 45 to the outside of the heat transfer tube of the heat exchanger 46.
  • the sprayed solution is heated by a heat source medium flowing in the heat transfer tube of the heat exchanger 46 and separated into a concentrated solution and refrigerant vapor.
  • the concentrated solution is guided to the auxiliary absorber 16 through the intermediate temperature solution heat exchanger 57 by the solution pump 54 installed in the middle of the solution pipe 51.
  • the refrigerant vapor separated from the concentrated solution is led to the condenser 40 through the baffle 52.
  • Heat source medium pipes 47 and 48 are connected to the heat exchanger 46 of the auxiliary regenerator 44.
  • the heat source medium is passed through the heat exchanger 35 of the high pressure regenerator 33, the heat exchanger 24 of the low pressure regenerator 22, and the heat exchanger 46 of the auxiliary regenerator 44 in this order, for example.
  • the heat source medium is utilized from a temperature higher than the solution temperature at the outlet of the high pressure regenerator 33 (about 90 ° C.) to a temperature close to the solution temperature at the outlet of the auxiliary regenerator 44 (about 60 ° C.). be able to.
  • the refrigerant flows down from the spraying device above each heat exchanger in the absorber 9, the low pressure regenerator 22, the high pressure regenerator 33, the auxiliary absorber 16, and the auxiliary regenerator 44. It is a liquid film heat exchanger.
  • the configuration of the present embodiment communicates the gas phase portion of the low-pressure regenerator 22 on the single effect cycle side and the auxiliary absorber 16 on the auxiliary absorption cycle side, and the high-pressure regenerator 33 and the condensation on the single-effect cycle side.
  • the gas phase section of the auxiliary regenerator 44 on the auxiliary absorption cycle side with the vessel 40, the single effect cycle and the auxiliary absorption cycle can be operated in combination.
  • an aqueous lithium bromide solution is used as the solution (absorbent), and water is used as the refrigerant.
  • the bottom surface 101 of the high pressure regenerator 33 is disposed higher than the bottom surface 102 of the low pressure regenerator 22 by a height H.
  • the height H is set so that the liquid level of the solution flowing out from the high pressure regenerator 33 during operation is formed in the pipe 49. This eliminates the need to store the solution in the high-pressure regenerator 33 during operation, thereby reducing the amount of refrigerant together with the amount of solution.
  • the liquid level of the low-pressure regenerator 22 is detected by a liquid level sensor (not shown) installed in the low-pressure regenerator 22, and if the liquid level drops, the spray amount is increased.
  • the flow rate adjustment valve 32 controls the spray amount to decrease, and the liquid level of the solution stored in the low pressure regenerator 22 is adjusted to a certain range.
  • the liquid level height of the solution flowing out from the high pressure regenerator 33 is the pressure difference ⁇ P1 generated between the high pressure regenerator 33 and the low pressure regenerator 22, and the high pressure regenerator 33 including the inside of the high temperature solution heat exchanger 56.
  • the liquid level height of the solution flowing out from the high pressure regenerator 33 can be reduced by the pressure difference ⁇ P1 with respect to the liquid level height in the low pressure regenerator 22, but is increased by the pressure loss ⁇ P2. If the liquid surface height of the solution stored in the low pressure regenerator 22 is 200 mm, the pressure difference ⁇ P1 is 200 mm, and the pressure loss ⁇ P2 is 1000 mm, the solution may be prevented from being stored in the high pressure regenerator 33.
  • the possible height H is H> 1000 mm.
  • the liquid level of the solution in the low-pressure regenerator 22, the pressure difference ⁇ P1 between the high-pressure regenerator 33 and the low-pressure regenerator 22, and the high-pressure regenerator 33 including the inside of the high-temperature solution heat exchanger 56 to the junction B The pressure loss ⁇ P2 of the pipe 49 can be easily obtained if the specifications and operating conditions of the pipe 49 and the high-temperature solution heat exchanger 56 are determined, and the high pressure regenerator from the bottom surface 102 of the low pressure regenerator 22 based on the result.
  • the height H to the bottom surface 101 of 33 can be set and the device arrangement can be determined.
  • the absorption refrigerator 100 of the present embodiment distributes the solution of the absorber 9 to the low pressure regenerator 22 and the high pressure regenerator 33 at the branch point A, and the solution from the low pressure regenerator 22 and the high pressure regenerator 33 is combined with the junction.
  • the solution is combined at B and is introduced into the absorber 9 by the solution pump 30.
  • the solution from the two elements, the low pressure regenerator 22 and the high pressure regenerator 33 flows into the solution pump 30.
  • the other elements are that the absorber 5 flows into the solution pump 14, the auxiliary absorber 16 enters the solution pump 19, and the solution from the auxiliary regenerator 44 flows into the solution pump 54.
  • , 62, 63, 64 are provided in a one-to-one relationship, and the tank is operated with a certain amount of solution stored in the tank. This is to allow a change in the amount of the solution due to the change in the concentration of the solution in the operating range and to prevent the liquid level in each solution tank from fluctuating sensitively.
  • the pressure can be secured, and each solution pump can be driven stably.
  • the solution from the high pressure regenerator 33 and the low pressure regenerator 22 flows into the solution pump 30, but in order to drive the solution pump 30 stably, the solution tank is the same as other elements. Since one is sufficient, the low pressure regenerator 22 is provided with a solution tank 63. In the low pressure regenerator 22, the pressure loss of the solution up to the solution pump 30 is smaller than that of the high pressure regenerator 33 via the high temperature solution heat exchanger 56, so that the solution tank 63 is provided in the low pressure regenerator 22. There is an effect that the liquid level required for the stable operation of the pump 30 can be kept low.
  • the bottom surface 101 of the high pressure regenerator 33 is arranged at a position higher than the bottom surface 102 of the low pressure regenerator 22 so that the liquid level of the solution flowing out from the high pressure regenerator 33 during operation is formed in the pipe 49.
  • the bottom of the high-pressure regenerator 33 was arranged so that no solution was collected during operation. This eliminates the need for a solution tank in the high-pressure regenerator 33 and reduces the amount of solution and the amount of refrigerant, thereby contributing to downsizing and cost reduction of the absorption refrigeration machine 100. Further, since the heat capacity of the retained liquid amount can be reduced by reducing the amount of solution and the amount of refrigerant, the start-up characteristics of the absorption chiller 100 can be improved.
  • Evaporator 9 Absorber 30: Solution pump 27, 49: Solution pipe 16: Auxiliary absorber 22: Low pressure regenerator 33: High pressure regenerator 40: Condenser 44: Auxiliary regenerator 56: High temperature solution heat exchanger 41 : Condenser 101: Bottom surface of high pressure regenerator 102: Bottom surface of low pressure regenerator

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Materials Engineering (AREA)
  • Power Engineering (AREA)
  • Sorption Type Refrigeration Machines (AREA)
PCT/JP2017/031613 2016-09-23 2017-09-01 吸収式冷凍機 WO2018056024A1 (ja)

Priority Applications (2)

Application Number Priority Date Filing Date Title
KR1020187009541A KR102017436B1 (ko) 2016-09-23 2017-09-01 흡수식 냉동기
CN201780003541.1A CN108139126B (zh) 2016-09-23 2017-09-01 吸收式冷冻机

Applications Claiming Priority (2)

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JP2016185021A JP6632951B2 (ja) 2016-09-23 2016-09-23 吸収式冷凍機
JP2016-185021 2016-09-23

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JP (1) JP6632951B2 (ko)
KR (1) KR102017436B1 (ko)
CN (1) CN108139126B (ko)
WO (1) WO2018056024A1 (ko)

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE112017006707B4 (de) * 2017-02-16 2023-10-19 Hitachi-Johnson Controls Air Conditioning, Inc. Absorptionskältemaschine
JP7154066B2 (ja) * 2018-08-29 2022-10-17 日立ジョンソンコントロールズ空調株式会社 吸収式冷凍機

Citations (4)

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JP2002349987A (ja) * 2001-05-30 2002-12-04 Mitsubishi Heavy Ind Ltd 吸収冷凍機
WO2004029524A1 (ja) * 2002-09-27 2004-04-08 Ebara Corporation 吸収冷凍機
KR100746241B1 (ko) * 2006-06-20 2007-08-03 한국지역난방공사 저온수 2단 흡수식 냉동기
JP2014196861A (ja) * 2013-03-29 2014-10-16 川重冷熱工業株式会社 吸収式冷凍機

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JP2000028236A (ja) * 1998-07-13 2000-01-28 Paloma Ind Ltd 吸収式冷凍機
JP3824436B2 (ja) * 1998-12-08 2006-09-20 荏原冷熱システム株式会社 三重効用吸収冷凍機
JP3603006B2 (ja) * 2000-04-28 2004-12-15 株式会社 日立インダストリイズ 吸収冷凍機及び吸収冷凍機の制御方法
JP2002048427A (ja) * 2000-08-02 2002-02-15 Hitachi Ltd 吸収冷凍機
JP2002081805A (ja) * 2000-09-08 2002-03-22 Hitachi Ltd ２段吸収冷凍機
CN100380069C (zh) * 2002-09-27 2008-04-09 株式会社荏原制作所 吸收式冷冻机
JP2004211979A (ja) 2003-01-06 2004-07-29 Ebara Corp 吸収冷凍システム
KR101042812B1 (ko) * 2009-04-10 2011-06-20 주식회사 센추리 2단 저온수 흡수식 냉동기
JP2010266170A (ja) * 2009-05-18 2010-11-25 Sanyo Electric Co Ltd 吸収式冷凍機
CN204063675U (zh) * 2014-09-16 2014-12-31 同方川崎节能设备有限公司 溴化锂吸收式机组循环系统

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2002349987A (ja) * 2001-05-30 2002-12-04 Mitsubishi Heavy Ind Ltd 吸収冷凍機
WO2004029524A1 (ja) * 2002-09-27 2004-04-08 Ebara Corporation 吸収冷凍機
KR100746241B1 (ko) * 2006-06-20 2007-08-03 한국지역난방공사 저온수 2단 흡수식 냉동기
JP2014196861A (ja) * 2013-03-29 2014-10-16 川重冷熱工業株式会社 吸収式冷凍機

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CN108139126B (zh) 2020-08-25
KR20180051566A (ko) 2018-05-16
KR102017436B1 (ko) 2019-10-14
JP2018048778A (ja) 2018-03-29
JP6632951B2 (ja) 2020-01-22
CN108139126A (zh) 2018-06-08

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