EP0887600A2 - Absorptionskälteanlage und entsprechendes Arbeitsverfahren - Google Patents

Absorptionskälteanlage und entsprechendes Arbeitsverfahren Download PDF

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Publication number
EP0887600A2
EP0887600A2 EP98111498A EP98111498A EP0887600A2 EP 0887600 A2 EP0887600 A2 EP 0887600A2 EP 98111498 A EP98111498 A EP 98111498A EP 98111498 A EP98111498 A EP 98111498A EP 0887600 A2 EP0887600 A2 EP 0887600A2
Authority
EP
European Patent Office
Prior art keywords
station
crystalliser
plant
absorption
heat exchanger
Prior art date
Legal status (The legal status 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 status listed.)
Withdrawn
Application number
EP98111498A
Other languages
English (en)
French (fr)
Other versions
EP0887600A3 (de
Inventor
Giancarlo Marelli
Vincenzo Longo
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Ldh Srl
Original Assignee
Ldh Srl
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 Ldh Srl filed Critical Ldh Srl
Publication of EP0887600A2 publication Critical patent/EP0887600A2/de
Publication of EP0887600A3 publication Critical patent/EP0887600A3/de
Withdrawn legal-status Critical Current

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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
    • F25B25/00—Machines, plants or systems, using a combination of modes of operation covered by two or more of the groups F25B1/00 - F25B23/00
    • F25B25/02—Compression-sorption machines, plants, or systems
    • 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
    • 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
    • F25B25/00—Machines, plants or systems, using a combination of modes of operation covered by two or more of the groups F25B1/00 - F25B23/00
    • F25B25/005—Machines, plants or systems, using a combination of modes of operation covered by two or more of the groups F25B1/00 - F25B23/00 using primary and secondary systems

Definitions

  • the invention concerns a perfected absorption cooling method and the working method relating thereto.
  • the core of these plants lies in a cooling thermal cycle which can take place in a compression circuit or an absorption circuit.
  • a cooling thermal cycle which can take place in a compression circuit or an absorption circuit.
  • it is a stable fluid with the appropriate characteristics which makes the cycle
  • Compression circuits are extremely complex in construction due to their particular power requirements or the minimum achievable temperature.
  • Absorption circuits could be more competitive if it were possible to re-use several evaporation stages in series, each one with a lower pressure than the previous one, but this is prevented by the high saline concentration: in fact the vapour pressure is lowered (the boiling temperature is increased) which prevents the application of a high number of evaporations.
  • the purpose of the invention is to overcome the shortcomings of the state of the art.
  • the object of the invention therefore is a perfected absorption cooling plant and the relative working method, which include simplicity of construction, considerable reliability and an optimum thermal yield.
  • an absorption cooling plant comprising a crystalliser, an evaporation station, an absorption station, a plurality of pumps, a plurality of heat exchangers, a refrigeration system and a saline solution which circulates inside and achieves the cooling cycle of the plant.
  • the working method relative to the plant according to the invention comprises a plurality of passes of a saline solution through a crystalliser, an evaporation station, an absorption station and a plurality of heat exchangers which, at every pass, modify the concentration of the saline solution thus making feasible the cooling cycle obtained with the plant according to the invention.
  • the perfected absorption cooling plant according to the invention is characterised by the fact that it includes the characteristics described in Claim 1.
  • the thermal yield obtained is decidedly greater than that of systems known to the state of the art, both those using compression circuits and those using absorption circuits.
  • a further advantage is that the entire plant is extremely reliable, and safe to manage and control.
  • Fig. 1 is a diagram of the perfected absorption cooling plant according to the invention.
  • Fig. 2 is a diagram of the plant shown in Fig. 1, using a different type of crystalliser.
  • Fig. 3 is a flow chart of the plant according to the invention applied to a vacuum distiller, which also shows the energy flows inside the plant according to the invention, wherefrom it can be seen that with a thermal power at inlet of 1.5 KCal thermal powers of 28.6 KCal are obtained.
  • Fig. 4 is another flow chart showing the energy flows inside the plant according to the invention.
  • Fig. 5 is a flow chart showing the percentage variation of the solute-solvent in a saline solution used inside the plant according to the invention.
  • the perfected absorption cooling plant and the relative working method according to the invention are based on the crystallisation of a solution and on the variations in concentration at the different points of the plant.
  • the solubility of a solid in its solvent increases with temperature and the solution is said to be saturated when it reaches the maximum concentration of the solute, as a balance is achieved between the dissolved substance and the substance present as a residue.
  • the solution in environment C which serves as a crystalliser, is cooled by a refrigeration or cooling system until the temperature of crystallisation is reached; this temperature varies according to the concentration and the solvent-solute pair.
  • the crystals thus obtained by means of the motorised valve VM arrive at the separator SC and are conveyed to the collector RC.
  • the crystal collector RC communicates with the exchanger SA of an absorption station A and with the exchanger SE belonging to an evaporation station E, which can be of different types.
  • the vapour generated in the exchanger SE comes into contact with the crystals and is absorbed, thus generating heat which is removed by a fluid circulating in the exchanger SA (points 3 and 4 of Figs. 1 and 2) to give maximum absorption.
  • the solution thus obtained is sent by means of the pump P1, after passing through the exchanger SCR3, to the crystalliser C in order to repeat the cycle (point 7).
  • vapours and the concentrated solution return to the crystalliser C (point 6) where they separate: the vapours are absorbed as previously described in the exchanger SA, while the concentrated solution, collected on the bottom, is sent by means of the pump P2 to the crystalliser C (point 8).
  • Figs. 1 and 2 show two variants of a crystalliser.
  • the solvent-solute pair used is water and sodium hydroxide (H 2 O - NaOH), but it is possible to use different solutions, such as for example water and lithium bromide and other saline solutions with characteristics similar to these.
  • the environment of the crystalliser C comprises two sections: a refrigeration section, where the solution is taken to the temperature of crystallisation, and the other to separate the crystals; the latter communicates with the exchangers SE and SA of the evaporation station E and the absorption station A, and is located above the two exchangers.
  • the refrigeration section is shaped like a truncated cone so as to allow the crystals to collect on the bottom and to convey them to the separator.
  • the solution arriving at the crystalliser C consists of two currents, one arriving from the exchanger SA of the absorption station A with a concentration of 66% of NaOH (equal to 100 parts of H 2 0 and 50 parts of NaOH in weight) at a temperature of 50°C, the other current from the exchanger SE of the evaporation station E with a concentration of 50% of NaOH (equal to 50 parts of H 2 0 and 50 parts of NaOH in weight) at a temperature of 30°C.
  • the concentration of the solution will fall to 33% NaOH (equal to 50 parts of H 2 0 and 100 parts of NaOH in weight) including, in the example in question, 100 parts (or grams) of NaOH crystals as residue.
  • the latter is enveloped, on the shell side, by saturated, condensing water vapours at a temperature of 48°C arriving from the exchanger SA of the absorption station A.
  • the solution continues to receive heat and can continue to evaporate until it reaches a new concentration of 50% NaOH (equal to 50 parts of H 2 O and 50 parts of NaOH in weight) at a temperature of 40°C.
  • the crystals generated arrive in the collector RC connected to the exchanger SA, and, since they are deliquescent and with a zero vapour pressure compared with that of water, the vapour is absorbed, and consequently heat is generated, so that the crystals return to a state of solution, absorbing the vapour (50g) generated in the exchanger SE.
  • the absorption heat in the exchanger SA is yielded to the water which begins to boil, generating vapour.
  • the concentration at outlet of the exchanger is 66% (equal to 100 parts H 2 0 and 50 parts of NaOH in weight).
  • the shape and size of the various elements comprising the perfected absorption cooling plant according to the invention, the solutions used, the temperatures, the pressures and the concentrations achieved, shall be able to vary according to the different requirements; however, the plant still remains within the field of the invention as described above.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Sorption Type Refrigeration Machines (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
EP98111498A 1997-06-24 1998-06-23 Absorptionskälteanlage und entsprechendes Arbeitsverfahren Withdrawn EP0887600A3 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
IT97MI001493A IT1292413B1 (it) 1997-06-24 1997-06-24 Impianto perfezionato di raffreddamento ad assorbimento e metodo funzionale relativo
ITMI971493 1997-06-24

Publications (2)

Publication Number Publication Date
EP0887600A2 true EP0887600A2 (de) 1998-12-30
EP0887600A3 EP0887600A3 (de) 1999-06-30

Family

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Family Applications (1)

Application Number Title Priority Date Filing Date
EP98111498A Withdrawn EP0887600A3 (de) 1997-06-24 1998-06-23 Absorptionskälteanlage und entsprechendes Arbeitsverfahren

Country Status (2)

Country Link
EP (1) EP0887600A3 (de)
IT (1) IT1292413B1 (de)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102287953A (zh) * 2011-06-23 2011-12-21 江苏河海新能源有限公司 简易溶解吸热式化学热泵及其加热或制冷方法

Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1541968A (en) * 1925-01-09 1925-06-16 Donald B Knight Refrigeration
US2182453A (en) * 1936-01-18 1939-12-05 William H Sellew Heat transfer process and apparatus
US3854301A (en) * 1971-06-11 1974-12-17 E Cytryn Cryogenic absorption cycles
DE2330216A1 (de) * 1973-06-14 1975-01-02 Hoehne Geb Kimmel Hanna Ursula Verfahren zum pumpen von waerme
US4051888A (en) * 1973-07-07 1977-10-04 Daikin Kogyo Co., Ltd. Low temperature energy carrying apparatus and method
US4100755A (en) * 1976-12-20 1978-07-18 Carrier Corporation Absorption refrigeration system utilizing solar energy
GB1534955A (en) * 1975-05-05 1978-12-06 Hastwell P Endothermic cooling system
US4413480A (en) * 1982-04-05 1983-11-08 Institute Of Gas Technology Hyperabsorption space conditioning process and apparatus
WO1986001880A1 (en) * 1984-09-13 1986-03-27 Gadd, Olof A chemo-thermal plant

Patent Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1541968A (en) * 1925-01-09 1925-06-16 Donald B Knight Refrigeration
US2182453A (en) * 1936-01-18 1939-12-05 William H Sellew Heat transfer process and apparatus
US3854301A (en) * 1971-06-11 1974-12-17 E Cytryn Cryogenic absorption cycles
DE2330216A1 (de) * 1973-06-14 1975-01-02 Hoehne Geb Kimmel Hanna Ursula Verfahren zum pumpen von waerme
US4051888A (en) * 1973-07-07 1977-10-04 Daikin Kogyo Co., Ltd. Low temperature energy carrying apparatus and method
GB1534955A (en) * 1975-05-05 1978-12-06 Hastwell P Endothermic cooling system
US4100755A (en) * 1976-12-20 1978-07-18 Carrier Corporation Absorption refrigeration system utilizing solar energy
US4413480A (en) * 1982-04-05 1983-11-08 Institute Of Gas Technology Hyperabsorption space conditioning process and apparatus
WO1986001880A1 (en) * 1984-09-13 1986-03-27 Gadd, Olof A chemo-thermal plant

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102287953A (zh) * 2011-06-23 2011-12-21 江苏河海新能源有限公司 简易溶解吸热式化学热泵及其加热或制冷方法
CN102287953B (zh) * 2011-06-23 2013-01-02 江苏河海新能源有限公司 简易溶解吸热式化学热泵及其加热或制冷方法

Also Published As

Publication number Publication date
IT1292413B1 (it) 1999-02-08
EP0887600A3 (de) 1999-06-30
ITMI971493A0 (de) 1997-06-24
ITMI971493A1 (it) 1998-12-24

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