WO1986002147A1 - Procede de refrigeration par absorption - Google Patents

Procede de refrigeration par absorption Download PDF

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Publication number
WO1986002147A1
WO1986002147A1 PCT/US1984/001585 US8401585W WO8602147A1 WO 1986002147 A1 WO1986002147 A1 WO 1986002147A1 US 8401585 W US8401585 W US 8401585W WO 8602147 A1 WO8602147 A1 WO 8602147A1
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WO
WIPO (PCT)
Prior art keywords
zone
component
refrigerant
cycle
water
Prior art date
Application number
PCT/US1984/001585
Other languages
English (en)
Inventor
Leon Lazare
Original Assignee
The Puraq Company
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 The Puraq Company filed Critical The Puraq Company
Priority to JP59503733A priority Critical patent/JPH0633911B2/ja
Priority to PCT/US1984/001585 priority patent/WO1986002147A1/fr
Priority to BR8407364A priority patent/BR8407364A/pt
Priority to IN706/CAL/84A priority patent/IN162757B/en
Publication of WO1986002147A1 publication Critical patent/WO1986002147A1/fr

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C09—DYES; PAINTS; POLISHES; NATURAL RESINS; ADHESIVES; COMPOSITIONS NOT OTHERWISE PROVIDED FOR; APPLICATIONS OF MATERIALS NOT OTHERWISE PROVIDED FOR
    • C09K—MATERIALS FOR MISCELLANEOUS APPLICATIONS, NOT PROVIDED FOR ELSEWHERE
    • C09K5/00—Heat-transfer, heat-exchange or heat-storage materials, e.g. refrigerants; Materials for the production of heat or cold by chemical reactions other than by combustion
    • C09K5/02—Materials undergoing a change of physical state when used
    • C09K5/04—Materials undergoing a change of physical state when used the change of state being from liquid to vapour or vice versa
    • C09K5/047—Materials undergoing a change of physical state when used the change of state being from liquid to vapour or vice versa for absorption-type refrigeration 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
    • F25B15/006—Sorption machines, plants or systems, operating continuously, e.g. absorption type with cascade 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
    • F25B15/02—Sorption machines, plants or systems, operating continuously, e.g. absorption type without inert gas
    • 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
    • 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
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency

Definitions

  • This invention relates to a highly efficient refrigeration system and process, driven by low-grade heat and operated at pressures substantially below atmospheric, which provides cooling at temperatures as low as about -10°C.
  • Solutions of normally liquid, mutually soluble components, having substantially dif ⁇ ferent boiling points, are employed as refrigerant and absorbent.
  • the absorbent comprises a dis ⁇ tillation bottoms fraction containing from about 65 to about 95 mol. % of the higher-boiling component and the refrigerant comprises a distillation overhead fraction containing from about 93 to about 99 mol. % of the lower- boiling component.
  • Multi-effect modes may be employed.
  • Absorption cooling processes in general, en- able thermal energy to be converted directly into a cooling effect and thus provide a basis for economic refrigeration processes.
  • the absorption cycle has been employed with only a few absorbent-refrigerant combinations although many com- ponents have been suggested based on their respective physical properties and on theoretical consideration of the absorption cycle.
  • refrigerant is first evaporated to afford a cooling effect, refrigerant vapor is then taken up in an absorbent, with evolution of heat, and finally the rich absorbent solution is subjected to fractionation to regenerate the refrigerant as an overhead stream for condensation and recyle to the evaporation step.
  • the absorption cooling process is usually op-
  • OMPI erated at or near atmospheric pressure An ideal re ⁇ frigerant has been defined as one permitting boiling o o at about 5 - 10 C. and absorption at about 38 C. or higher.
  • An ideal absorbent should be a liquid having a relatively high boiling point.
  • a suitable refrigerant- absorbent combination should exhibit a significant negative deviation in vapor pressure from an ideal solu ⁇ tion.
  • Commercial utilization has been generally limited to two systems, one employing water as refrigerant with lithium bromide brine as absorbent, and the other em ⁇ ploying ammonia as refrigerant with aqueous ammonia as the absorbent.
  • the efficiency of an absorption cycle is dependent only upon the temperature levels achieved in the evaporator, absorber, regenerator and condenser sections of the cycle.
  • the per ⁇ missible operating temperatures for these sections ex ⁇ hibit an interdependence which serves to limit the ef ⁇ fective performance of the system.
  • the refrigerant partial pressure in the absorber will de ⁇ termine the operating temperature in the evaporator.
  • the refrigerant partial pressure in the regenerator will determine the temperatures in the condenser.
  • the operating temperatures in the eva- porator and condenser are fixed by the temperatures and concentrations maintained in the absorber and regenera ⁇ tor.
  • OMPI as 0 C.
  • Ammonia-aqueous ammonia systems are often employed despite their generally low coefficients of performance; these systems have greater flexibility in the choice of operating conditions and are not subject to the possibilities of crystallization and icing.
  • absorption refrigeration as an al ⁇ ternative to electrically-driven or steam-turbine driven mechanical refrigeration, the choice has generally been limited by economic considerations involving the sel- e ⁇ tive use of a particular form of energy rather than another.
  • OMP n-propyl alcohol, ethylene diamine, n-amyl amine, morpholine, and N-methyl morpholine
  • U.S. Patent No. 1,734,278 discloses, as an improvement over the ammonia-water absorption system, the use of a methyl amine as refrigerant and an al ⁇ cohol, such as glycerine, as the absorbent, particularly when having dissolved therein a metal salt of calcium barium, or lithium.
  • U.S. Patent No. 1,914,222 dis ⁇ closes ethylene glycol, alone or in mixture with water, as absorbent for use ' with methylamine as refrigerant. Hydrogen is present as an auxiliary gas.
  • U.S. Patent No. 1,953,329 discloses means for avoiding the freezing of the refrigerant by mixing with a minor quantity of the absorbent agent in the evaporator zone.
  • U.S. Patent No. 1,955,345 discusses problems with an am ⁇ monia - water system, such as the evaporation of water with ammonia and consequent loss of efficiency.
  • U.S. Patent No. 1,961,297 discloses apparatus for use with a water-glycerol mixture at sub-atmospheric pressures.
  • U.S. Patent No. 2,308,665 discloses water or low-boiling alcohol as refrigerant, and a polyamine or polyamide as absorbent and cites the methyl amine- ethylene glycol system.
  • U.S. Patent No. 2,963,875 discloses a heat pump system, employing liquids miscible at elevated temperatures, such as triethyl amine-water.
  • U.S. Patent No. 3,296,814 employs lithium salt solutions as absorbents, typically lithium bromide 5 in ethylene glycol-water.
  • U.S. Patent No. 3,388,557 clajlms as an absorbent a solution of lithium iodide in ⁇ " ethylene glycol-water.
  • U.S. Patent No. 3,524,815 dis ⁇ closes water as refrigerant with an absorbent com ⁇ prising lithium bromide and iodide, water, and ethylene
  • U.S. Patent No. 4,127,010 discloses a heat pump apparatus wherein the absorber liquor is pre ⁇ heated during passage to the evaporator by heat ex-
  • U.S. Patent No. 4,193, 268 discloses an evaporation device which permits a controlled evaporation rate in response to internal pressure differentials.
  • the heat transfer medium may
  • refrigerants 20 comprise water containing a minor amount of ethylene glycol.
  • Preferred refrigerants include various chloro- fluoromethanes and ammonia. Provision is made for injection of evaporator bottoms into a precooler other ⁇ wise containing refrigerant being passed to the ab-
  • the system of this invention relates to a cyclic absorption refrigeration system, employing
  • This invention additionally relates to the inclusion of a double-effect fractionation zone, each effect having at least two theoretical plates (as in sub-paragraph (c) above) , and wherein the operating pressure of the first effect is sufficiently greater than that of the second effect so that the latent heat of condensation which is released in the over-head con ⁇ denser of the first effect is employed to reboil the bottoms of the second effect.
  • the evaporation and absorption zones may be operated preferably at from about 2 to about 13 mm. mercury, absolute pressure, such that the evaporation zone may be maintained desirably at a temperature within the range from about -12 to about +15 C.
  • the reboiler section of the fractionation zone is desirably heated through heat-exchange surfaces with a waste heat stream, such as low-pressure steam or a warm process stream.
  • Low-boiling compounds for use in this in- vention include water, methanol, and acetone. Suitable
  • O H high-boiling compounds include ethylene glycol, prdpy- lene glycols, ethanolamine, diethylene glycol, butyrol- actone, and dimethyl formamide.
  • This invention additionally relates to a 5 refrigeration process and to a modified process em ⁇ ploying the system outlined above in serial operation with an ammonia-aqueous ammonia refrigeration process.
  • Figure 1 presents a simplified schematic
  • Figure 2 presents a similar representation employing two fractionation effects.
  • Figure 1 presents schematically a simplified flow-sheet illustrating one version of the process or system of this invention. Contained within vessel 1 are evaporation zone 2 and absorption zone 3. The second major vessel 4 comprises the fractionation zone.
  • Cooled liquid refrigerant component flows from evaporation zone 2 through lines 21, 22, and 23 to heat exchanger 6 where external fluid, passing through lines 75 and 76 is cooled indirectly. Liquid refrig ⁇ erant component, warmed in this manner by a few de-
  • the absorbent component, enriched with re ⁇ frigerant component in zone 3 is passed through line 39, pump P-l , and line 39a, and recycled in part to zone 3 after passage through line 57, heat exchanger 8, and lines 58, 55, 56, throttle valve V-l, and line 56a.
  • the remaining part is directed through line 40, heat exchanger 10, and lines 41, 42, and 43 to fractionation zone 4.
  • a portion of the fractionator bottoms is re- boiled by passage through lines 33, 34, 35, heat ex- changer 8, and lines 36 and 37 with reboiling effected indirectly in exchanger 7 with waste steam entering through line 70 and exiting as condensate through line 71.
  • any warm stream may be used, entering through line 70 and leaving through line 71 at a lower temperature.
  • a portion of the refrigerant component is directed through lines 21, 22, 26, 27 pump P-2, lines 27a and 28, heat exchanger 11, and lines 29, 30, 31, and 32 into the upper section of fractionation zone 4 as reflux.
  • the bottoms from zone 4, comprising absorbent component, is returned to absorption zone 3 by passage successively through lines 50, 51 and 52 heat exchanger 10, and lines 53, 54, 55, 56, valve V-l, and line 56a.
  • pumps may be employed in lines 34 and 51.
  • FIG. 2 presents schematically a simplified flowsheet illustrating a version of the process or system of this invention employing two fractionation effects, or stages.
  • Contained within vessel 101 are evaporation zone 102 and absorption zone 103.
  • Other major vessels include first fractionation effect 104 and second fractionation effect 105.
  • Cooled liquid refrigerant component flows from evaporation zone 102 through lines 121, 122, and 123 to heat exchanger 106, line 123a and heat exchanger 106a where external fluids, passing through lines 175 and 176, or lines 175a and 176a are cooled indirectly.
  • Refrigerant component additionally passes through lines 124 and 125 for return to an upper portion of zone 102 for admixture with vapors rising within vessel 101 and subsequently being passed into absorption zone 103 for admixture with absorbent component present therein.
  • the absorbent component, enriched with re ⁇ frigerant component in zone 103 is passed through line 139, pump P-101, and line 139a, and recycled in part to zone 103 after passage through line 157, heat exchanger 108, and lines 158, 155, 156, throttle valve V-l01, and line 156a.
  • the remaining part is directed through line 140, heat exchanger 110, and lines 141, 142, and 143, heat exchanger 113, and line 143a to fractionation zone 104.
  • a portion of the fractionator bottoms from zone 104 is reboiled by passage through lines 133, 134, 135, heat exchanger 107, and lines 136 and 137, with reboiling effected indirectly in exchanger 107 with waste steam entering through line 170 and exiting as condensate through line 171, or alternatively with a warm process stream which exits through line 171 at a lower temperature than in line 170.
  • a portion of the refrigerant component is directed through lines 121, 122, 126, 127, pump P-102, lines 127a and 128, heat exchanger 111, and lines 129, 130, 131, and 132 into the upper section of fractionation zone 104 as reflux.
  • the bottoms from zone 104 is directed to second fractionation zone 105 by passage successively through lines 150, 151, and 152, heat exchanger 113, and lines 191 and 191a.
  • a portion of the fractionator bottoms from zone 105 is reboiled by passage through lines 195, 196, 197, heat exchanger 112, and lines 198 and 198a, with reboiling effected indirectly in exchanger 112 with overhead vapors from first fractionator 104 which enter exchanger 112 through lines 138 and 138a and exit through lines 138b, 144 and 145.
  • the bottoms from zone 105 comprising absorbent component, is returned to absorption zone 103 by pas ⁇ sage successively through lines 192, 193, 194, heat exchanger 110, and lines 153, 154, 155, 156, throttle valve V-101, and line 156a.
  • the overhead vapor stream from zone 105 exits through line 181, merges with the liquid stream from exchanger 112 through line 145, and the combined streams, comprising refrigerant component, are re ⁇ turned to evaporation zone 103 by passage successively through lines 145a, 146, heat exchanger 109, lines 147, 182, 183, heat exchanger 114, lines 148, 148a, heat exchanger 111, line 149, throttle valve V-102, and line 149a.
  • Cooling is effected in heat exchangers 108 and 109 by indirect cooling with a water stream from water source 160, passing through line 161, exchanger 108, lines 162 and 162a, exchanger 109, and water ef ⁇ fluent line 163.
  • a portion of the water stream is di ⁇ verted through lines 164 and 165, exchanger 114, and lines 166 and 167, finally merging with the main stream in line 162 and continuing through line 162a.
  • pumps may be employed in any or all of lines 134, 151, 193 and 196.
  • This invention relates to a cyclic absorption refrigeration system and to a refrigeration process employing the aforesaid system, driven by low-grade heat and operated at pressures substantially below atmospheric. Cooling to temperatures as low as about -10°C. may be realized while temperatures of about -5 C. are readily achieved.
  • the invention relates to a cyclic absorption refrigeration system, employing mutually soluble, normally liquid compounds in each of absorbent and refrigerant components, com- prising:
  • a fractionation zone operating at a second, higher sub-atmospheric pressure, having a separation efficiency equivalent to at least about two theoretical plates; wherein the liquid compounds have normal boiling points differing by at least about 50 C; the absorbent component comprises from about 65 to about 95 mol. % of the higher-boiling compound; and the refrigerant component comprises from about 93 to about 99 mol. % of the lower-boiling compound.
  • This invention permits the use of absorption refrigeration as a tool for energy conservation whereby waste heat is converted to utilizable refrigeration. Additionally, current striking increases in energy
  • the evapora- tion and absorption zones are generally maintained at a low sub-atmospheric pressure within the range from about 2 to about 13 mm. mer ⁇ ury absolute pressure, and preferably within the range from about 3 to about 9 mm. mercury absolute pressure.
  • the fractionation zone is maintained at a higher sub-atmospheric pressure, generally within the range from about 30 to about 150 mm. mercury absolute pressure, and preferably within the range from about 30 to about 100 mm. mercury absolute pressure.
  • absorbent and refrigerant component compositions may be achieved which permit the maintenance of a temperature in the evaporation zone (flash refrigeration level) within the range from about -12 to about +15 C, and preferably from about -5 to about +10 C.
  • the cor ⁇ responding temperature in the absorption zone is gen ⁇ erally maintained within the range from about 20 to about 60°C. , and preferably from about 30° to about 40°C.
  • the fractionation zone reboiler section is maintained at a temperature within the range from about 65 to about 110 C. , and preferably from about 75 to about 95 C. , by indirect heat exchange with an external source of heat.
  • the fractionation zone need not be highly efficient, a separation efficiency of about three or four theoretical plates being sufficient.
  • Some reflux is provided in the upper section of the fractionator with a purge stream taken from the evaporation zone.
  • an improved degree of ef ⁇ fectiveness may be achieved by inclusion of a second fractionation zone.
  • the rich ab ⁇ sorbent component is directed to a first fractionator operating at a higher pressure, usually within the range from about 250 to about 760 mm. mercury ab ⁇ solute pressure, and preferably from about 300 to about 650 mm. mercury absolute pressure.
  • Bottoms from the first fractionator is fed to a second fractionator operating substantially as described earlier above, except that its reboiler duty is provided by heat ex ⁇ change with overhead vapors from the first fractionator.
  • the first fractionator derives heat from a reboiler system, now maintained at a temperature gen- erally within the range from about 110 to about 150 C, and preferably from about 120° to about 140 C, by indirect heat exchange with an external source of heat. If desired, still further fractionation effects may be employed although two will usually suffice.
  • the temperature level achieved in the evapora ⁇ tion zone permits refrigeration of an external stream, by indirect heat exchange with the chilled liquid re ⁇ frigerant component, to a temperature preferably within the range from about -8 to about +20 C. , and most preferably from about -3 to about +15 C.
  • external stream may include ' ammonia, brines, petrochemical or petroleum process stream, - n & the like.
  • normally liquid compounds are generally suitable for use in the system and process of this invention. All must be stable, non-corrosive, and completely miscible one with another.
  • the normal boiling points of the lower-and higher- boiling compounds of a selected pair should differ by
  • the lower-boiling compound is preferably water, although acetone methanol, or mix ⁇ tures of any of these may be employed.
  • the higher- boiling compound is preferably ethylene glycol, al- though such compounds as 1,3-propylene glycol, 1,2- propylene glycol, diethylene glycol, butyrolactone, dimethyl formamide, mono-ethanolamine, or mixtures of any of these may be used.
  • other promising systems include acetone-butyrolactone, methanol-l,2-propylene glycol, and methanol-1,3-propylene glycol.
  • the attractive utility of this refrigera ⁇ tion system derives in part from the discovery that neither of the selected absorbent and refrigerant components need comprise substantially pure compounds, thus limiting the fractionation requirements and making possible the selection of compound combinations which in the past have evoked only speculation without the discernment of effective means for efficient and economic utilization.
  • the refrigerant component need only comprise from about 93 to about 99 mole %, preferably about 96 mole %, of the lower-boiling compound.
  • the absorbent component need only comprise from about 65 to about 95 mole % preferably from about 75 to about 90 mole %, of the higher-boiling compound.
  • cooling water at ambient temperature is also employed to remove heat from the overhead vapors from the fractionation zone or from recycled absorbent com ⁇ ponent (see heat exchangers 9 and 8, respectively, as set forth in Figure 1) .
  • the thermal efficiency, or coefficient of performance (C.O.P.), of an absorption cycle is de- fined as the ratio of the cooling effect to the energy in-
  • the CO.P. is the ratio of refrigeration by the evapora ⁇ tor to the heat input to the generator, or fractionator.
  • refrigerant component containing about 98 mole % water and about 2 mole % ethylene glycol, is flashed at about 3 mm. mercury absolute pressure in the evaporation zone to produce a flash refrigeration level of about -5 C.
  • an external stream may be cooled by indirect heat exchange to a temperature of about -3 C.
  • the major portion of the water-enriched ab- sorbent component is re-concentrated in a fractionation zone, comprising one theoretical stripping plate and two theoretical rectifying plates, at a pressure of about 52 mm. mercury and a reboiler temperature of about 81 C. , with the refrigerant component, comprising about 98 mole % water and about 2 mole % ethylene glycol, being recovered as the overhead product and returned to the evaporation zone.
  • Reflux to the fractionation zone is provided by directing a slipstream from the evaporation zone bottoms to the upper portion of the fractionator.
  • the heat of condensation of the overhead product is rejected to cooling water at about 34°C.
  • Heat to the reboiler is provided by heat exchange with low-pressure steam available at about 110°C.
  • the fractionator bot ⁇ toms or absorbent component comprising about 85 mole % ethylene glycol and about 15 mole % water, is returned to the absorption zone after heat exchange with the water-rich effluent from the absorption zone.
  • the added fractionator is operated at the higher pressure of about 440 mm. mercury and the overhead vapors are cooled by reboiling the first frac ⁇ tionator. Bottoms from the second fractionator are at a temperature ofabout 131° C.
  • Reboiler duty is provided by a higher quality waste steam available at about
  • this second preferred embodiment only one of the fractionators is reboiled with an external heat source, such as low-pressure steam, so that the quantity of regeneration heat is reduced by at least about 40%.
  • a surprising advantage for the double-effect operation is the permissible regeneration employing low-pressure steam, derived from a back-pressure steam turbine at about 3_.5 -4.0 atmospheres or extracted at such a pressure from a totally condensing steam turbine.
  • the C.O.P of 1.47 is so high that the mechanical energy forfeited by not totally condensing the regeneration steam in the turbine system (at approximately 0.10 to 0.15 atmospheres) is less than one-half that which would be required to provide the refrigeration load of 1,000,000 BTU/hr. at -4°C. when employing a mechanical refrigeration unit.
  • a widely used absorption cooling cycle con ⁇ sists of ammonia as refrigerant and aqueous ammonia as absorbent, sometimes with hydrogen gas present as a third phase.
  • water must be removed from the re ⁇ frigerant component recovered as over-head vapor from the generator, or fractionator, zone.
  • ammonia is boiled from a solution at about 140 C and about 175 p.s.i.a.
  • the ammonia is condensed at about 35 C and transferred to an evapora ⁇ tion zone after throttling to about 760 mm. mercury pressure absolute.
  • the flash evaporation level achieved under these conditions is about -33 C
  • the absorbent solution now at about 35 C, is pumped back to the fractionator and recycled.
  • Heat is removed from both the fractionation zone condenser and from the absorption zone effluent by indirect heat exchange with cooling water.-
  • the coefficient of performance (C.O.P.) is within the range from about 0.1 to about 0.3.
  • the hybrid process of this invention effective ⁇ ly combines the novel process, described above in de- tail, with the ammonia-aqueous ammonia process by em ⁇ ploying the cooled refrigerant component of the novel process to withdraw heat from the ammonia process fractionator zone overhead and absorbent zone ef ⁇ fluent. This effectively removes the refrigerant com- ponent (ammonia) heat of condensation and its heat of
  • the cool ⁇ ant supplied at cooling source 60 is the refrigeration zone bottoms from, for example, an ethylene glycol- water process, rather than a cooling water stream. In this manner the coolant temperature can be lowered, for example, from about 35 C to about 5 C
  • Refrigeration Load BTU/hr. , 000 , 000 1 , 000 , 000 Refrigeration temp., C -18 -33 Coolant temp., C 3 3 Regeneration temp., C 35 55 Coefficient of Performance, C.O.P. 0. 79 0 . 67
  • the refrigeration system of this invention may also be employed serially with any suitable mech ⁇ anical refrigeration system to afford an economically and technically attractive means for achieving unusually low temperatures.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Chemical & Material Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Combustion & Propulsion (AREA)
  • Materials Engineering (AREA)
  • Organic Chemistry (AREA)
  • Sorption Type Refrigeration Machines (AREA)
  • Gas Separation By Absorption (AREA)

Abstract

Un système et un procédé de réfrigération extrêmement efficaces sont commandés par de la chaleur de basse teneur (70-71, 170-171) et fonctionnent à des pressions sensiblement sous-atmosphériques, fournissant un refroidissement jusqu'à des températures comprises généralement dans une plage allant de -12oC environ jusqu'à +15oC environ. Des solutions de composés normalement liquides et mutuellement solubles, ayant des points d'ébullition sensiblement différents, sont utilisés comme réfrigérant et comme absorbant. Typiquement, l'absorbant comprend une fraction de queue de distillation contenant entre 65 environ et 95 environ moles pour cent du composé dont le point d'ébullition est le plus élevé, et le réfrigérant comprend une fraction de tête de distillation contenant entre 93 environ et 99 environ moles pour cent du composé dont le point d'ébullition est le moins élevé. Des modes à effets multiples peuvent être employés. L'invention porte également sur l'utilisation de ce nouveau système de réfrigération dans un système et un procédé modifiés de réfrigération, dans lequel deux cycles de réfrigération par absorption sont utilisés en série. Le premier cycle comprend un système ammoniaque à l'ammoniaque liquide, et le deuxième cycle comprend ces nouveaux système et procédé d'absorption. La chaleur pompée pendant le premier cycle ammoniaque est absorbée pendant le deuxième cycle par le réfrigérant à la température de refroidissement obtenue dans celui-ci.
PCT/US1984/001585 1984-10-04 1984-10-04 Procede de refrigeration par absorption WO1986002147A1 (fr)

Priority Applications (4)

Application Number Priority Date Filing Date Title
JP59503733A JPH0633911B2 (ja) 1984-10-04 1984-10-04 吸収冷凍法
PCT/US1984/001585 WO1986002147A1 (fr) 1984-10-04 1984-10-04 Procede de refrigeration par absorption
BR8407364A BR8407364A (pt) 1984-10-04 1984-10-04 Processo de refrigeracao por absorcao
IN706/CAL/84A IN162757B (fr) 1984-10-04 1984-10-08

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PCT/US1984/001585 WO1986002147A1 (fr) 1984-10-04 1984-10-04 Procede de refrigeration par absorption

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WO1986002147A1 true WO1986002147A1 (fr) 1986-04-10

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BR (1) BR8407364A (fr)
IN (1) IN162757B (fr)
WO (1) WO1986002147A1 (fr)

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JP7261563B2 (ja) * 2018-11-02 2023-04-20 谷川油化興業株式会社 熱交換媒体

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3555841A (en) * 1968-07-15 1971-01-19 Trane Co Arsenic trioxide corrosion inhibitor for absorption refrigeration system
US3817050A (en) * 1972-12-26 1974-06-18 Texaco Inc Two-stage ammonia absorption refrigeration system with at least three evaporation stages
US4294076A (en) * 1979-05-30 1981-10-13 Sanyo Electric Co. Ltd. Absorption refrigerating system
US4363219A (en) * 1980-03-17 1982-12-14 Hitachi, Ltd. Method and system of heat energy conversion

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3555841A (en) * 1968-07-15 1971-01-19 Trane Co Arsenic trioxide corrosion inhibitor for absorption refrigeration system
US3817050A (en) * 1972-12-26 1974-06-18 Texaco Inc Two-stage ammonia absorption refrigeration system with at least three evaporation stages
US4294076A (en) * 1979-05-30 1981-10-13 Sanyo Electric Co. Ltd. Absorption refrigerating system
US4363219A (en) * 1980-03-17 1982-12-14 Hitachi, Ltd. Method and system of heat energy conversion

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JPS62500679A (ja) 1987-03-19
BR8407364A (pt) 1987-01-06
JPH0633911B2 (ja) 1994-05-02
IN162757B (fr) 1988-07-09

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