Serial absorption refrigeration process

• US 4,475,353 A
• Filed: 06/16/1982
• Issued: 10/09/1984
• Est. Priority Date: 06/16/1982
• Status: Expired due to Fees

• Current Assignee: Puraq As
• Original Assignee: Puraq As
• Inventors: Lazare, Leon
• Primary Examiner(s): King, Lloyd L.
• Application Number:
  US06/388,801
• Time in Patent Office: 846 Days
• Field of Search: 62/101, 62/112, 62/476, 62/475
• US Class Current: 62/101
• CPC Class Codes: F25B 15/006 with cascade operation
• CPC Class Codes: Y02A 30/27 Relating to heating, ventilation or air conditioning [HVAC] technologies
• CPC Class Codes: Y02B 30/62 Absorption based systems

Abstract

This invention relates to a highly efficient refrigeration system and process, employing two absorption refrigeration cycles in series operation, the first cycle comprising an ammonia-aqueous ammonia system and the second cycle comprising a novel absorption system and process, driven by low-grade heat and operated at pressures substantially below atmospheric, which provides cooling at temperatures as low as about -12° C. to about +15° C. Solutions of normally liquid, mutually soluble compounds, having substantially different boiling points, are employed as refrigerant and absorbent. Typically, the absorbent comprises a distillation bottoms fraction containing from about 65 to about 95 mole % of the higher-boiling compound and the refrigerant comprises a distillation overhead fraction containing from about 93 to about 99 mol. % of the lower-boiling compound. Heat pumped up in the first ammonia cycle is absorbed in the second cycle by refrigerant at the coolant temperature achieved therein.

Claims

1. A cyclic absorption refrigeration process, employing, in a first absorption refrigeration cycle, in a refrigerant component and in an absorbent component, mutually soluble, normally liquid compounds, whose normal boiling points differ by at least about 50°

C., and in a second absorption refregeration cycle, substantially anhydrous ammonia as refrigerant component and aqueous ammonia, containing from about 40 to about 70 wt. % water, as absorbent component, comprising the steps of;

(a) rectifying a refrigerant-enriched absorbent component, in a first-cycle fractionation zone, to provide an overhead refrigerant component stream, comprising from about 93 to about 99 mole % of the lower-boiling compound and from about 1 to about 7 mole % of the higher-boiling compound, and a bottoms absorbent component stream, comprising from about 65 to about 95 mole % of the higher-boiling compound and from about 5 to about 35 mole % of the lower-boiling compound, at a reflux zone pressure within the range from about 30 to about 150 mm. mercury absolute pressure, and at a reboiler zone temperature within the range from about 65 to about 110°

C., the reboiler zone being supplied, by indirect heat exchange, with heat from an external source of low-grade heat;

(b) cooling the overhead refrigerant component stream by indirect heat exchange with an external coolant stream;

(c) transferring the cooled overhead refrigerant component stream to a first-cycle evaporation zone;

(d) cooling the bottoms absorbent component stream by indirect heat exchange with the refrigerant-enriched absorbent component stream;

(e) transferring the cooled bottoms absorbent component stream to a first-cycle absorption zone.

(f) evaporating a substantial portion of the refrigerant component in the first-cycle evaporation zone maintained at a pressure within the range from about 2 to about 13 mm. mercury absolute pressure, to achieve a temperature in a remaining portion of the refrigerant component within the range from about -12°

to about +15°

C.;

(g) collecting an ammonia-water effluent mixture as enriched absorbent component from a second-cycle absorption zone;

(h) rectifying the ammonia-water mixture in a second-cycle fractionation zone to provide an overhead refrigerant component stream, comprising substantially anhydrous ammonia, and a bottoms absorbent component stream, comprising aqueous ammonia;

(i) circulating the remaining portion of the refrigerant component to a first-cycle refrigeration zone where, by indirect heat exchange, second-cycle ammonia overhead and ammonia-water effluent mixture are cooled to a temperature within the range from about -8°

to about +20°

C.

(j) conducting the evaporated portion of the refrigerant component to the first-cycle absorption zone for mixing therein with the absorbent component to provide the refrigerant-enriched absorbent component, said absorption zone being maintained at the same pressure as the evaporation zone and at a temperature within the range from about 20°

to about 60°

C., by continuously cooling a portion of the refrigerant-enriched absorbent component in indirect heat exchange with the external coolant stream;

(k) returning the refrigerant-enriched absorbent component to the first-cycle fractionating zone;

(l) continuously withdrawing a minor part of the refrigerant component from the first-cycle evaporation zone and injecting said refrigerant component into the first-cycle reflux zone;

(m) evaporating a substantial portion of the anhydrous ammonia in the second-cycle evaporation zone to achieve a temperature in the remaining liquid ammonia within the range from about -15°

to about -60°

C.; and

(n) circulating the remaining liquid ammonia to a second-cycle refrigeration zone where, by indirect heat exchange, an external heat exchange fluid is cooled to a temperature within the range from about -10°

to about -55°

C.

2. The process of claim 1 wherein the lower-boiling compound is selected from the class consisting of water, methanol, acetone, and mixtures thereof.

3. The process of claim 1 wherein the higher-boiling compound is selected from the class consisting of ethylene glycol;

diethylene glycol;

1,3-propylene glycol;

1,2-propylene glycol;

butyrolactone;

dimethyl formamide;

monoethanolamine; and

mixtures thereof.

4. The process of claim 1 wherein the lower-boiling compound is water and the higher-boiling compound is ethylene glycol.

5. The process of claim 1 wherein the lower-boiling compound is acetone and the higher-boiling compound is butyrolactone.

6. The process of claim 1 wherein the lower-boiling compound is methanol and the higher-boiling compound is 1,2-propylene glycol or 1,3-propylene glycol.

7. The process of claim 1 wherein the first-cycle fractionation zone comprises a plurality of stages, the added stages operating at successively higher reboiler temperatures;

the reboiler duty of the highest-pressure stage being provided by an external source of low-grade heat;

said highest-pressure stage processing the refrigerant-enriched absorbent component from the first-cycle absorption zone;

each successive lower-pressure stage processing the bottoms stream from the next-higher-pressure stage;

the reboiler duty to each successive lower-pressure stage being afforded by the overhead refrigerant component stream from the preceding stage;

the overhead streams from each stage being collected for transfer to the first-cycle evaporation zone; and

the bottoms stream from the lowest-pressure stage being transferred to the first-cycle absorption zone.

8. A serial absorption refrigeration process comprising the steps of:

(a) fractionating in a first absorption refrigeration cycle a water-ethylene glycol mixture, to provide a first-cycle overhead refrigerant component, comprising about 98 mole % water and about 2 mol. % ethylene glycol, and a first-cycle bottoms absorbent component, comprising about 85 mol. % ethylene glycol and about 15 mol. % water, at a reflux pressure of about 50 mm. mercury absolute and a reboiler temperature of about 85°

C., in indirect heat exchange with an external source of low grade steam;

(b) fractionating in a second absorption refrigeration cycle a water-ammonia mixture, to provide a second-cycle overhead refrigerant component, comprising substantially anhydrous ammonia, and a second-cycle bottoms absorbent component, comprising about 38 mole % ammonia and about 62 mole % water, at a reflux pressure of about 75 p.s.i.a. and a reboiler temperature of about 60°

C.;

(c) cooling the first-cycle overhead refrigerant component with an external cooling water source and transferring the cooled component to a first-cycle evaporation zone;

(d) transferring the first-cycle bottoms absorbent component to a first-cycle absorption zone;

(e) evaporating a substantial portion of the refrigerant component in the first-cycle evaporation zone, at a pressure of about 5 mm. mercury absolute to provide a temperature level in the residual portion thereof of about 5°

C.;

(f) absorbing the evaporated portion of the refrigerant component in the absorbent component in the first-cycle absorption zone, at a pressure of about 5 mm. mercury absolute and at a temperature maintained at about 35°

C. by indirect heat exchange of the enriched absorbent component with an external cooling water source;

(g) returning the water-ethylene glycol product of the absorption step (f) to the fractionating step (a);

(h) cooling the second-cycle ammonia overhead refrigerant to a temperature of about 5°

C. in indirect heat exchange with the residual refrigerant component from step (e);

(i) transferring the second-cycle water-ammonia bottoms absorbent component to a second-cycle absorption zone;

(j) evaporating a substantial portion of the ammonia in the second-cycle evaporation zone, at a pressure of about 760 mm. mercury absolute to provide a second-cycle refrigeration temperature in the residual portion thereof of about -33°

C.;

(k) absorbing the evaporated ammonia in the second-cycle absorbent component in the second-cycle absorption zone at a pressure of about 760 mm. mercury absolute and at a temperature maintained at about 5°

C. by indirect heat exchange of the enriched absorbent component with the residual refrigerant component from step (e);

(1) returning the ammonia-water product of the absorption step (k) to the fractionating step (b); and

(m) withdrawing a portion of the residual refrigerant component from the first-cycle evaporation zone and injecting said portion as reflux into the first-cycle fractionating step (a).

9. The process of claim 8 wherein there is provided a second-cycle refrigeration temperature within the range from about -15°

to about -40°

C.

10. In a refrigeration system, comprising a first cyclic absorption refrigeration system, having as refrigerant substantially anhydrous ammonia, and as absorbent aqueous ammonia, containing from about 30 to about 60 wt. % ammonia and from about 40 to about 70 wt. % water, the improvement comprising the removal of heat therefrom to a second cyclic absorption refrigeration system employed serially with the first ammonia-aqueous ammonia system, whereby heat is withdrawn from the first system at substantially the refrigerant cooling temperature of the second system, said second cyclic absorption refrigeration system employing mutually soluble, normally liquid compounds in each of absorbent and refrigerant components, and comprising:

(a) an evaporation zone, operating at a first, low atmospheric pressure;

(b) an absorption zone, operating at the first low sub-atmospheric pressure; and

(c) 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.

11. The refrigeration system of claim 10 wherein a purge stream from the evaporation zone is continuously introduced into a reflux section of the fractionation zone.

12. The refrigeration system of claim 10 wherein the first, low sub-atmospheric pressure is maintained within the range from about 2 to about 13 mm. mercury absolute pressure.

13. The refrigeration system of claim 10 wherein the second, higher sub-atmospheric pressure is maintained within the range from about 30 to about 150 mm. mercury absolute pressure.

14. The refrigeration system of claim 10 wherein the evaporation zone is maintained at a temperature within the range from about -12°

to about +15°

C.

15. The refrigeration system of claim 10 wherein the absorption zone is maintained at a temperature within the range from about 20°

to about 60°

C.

16. The refrigeration system of claim 10 wherein the fractionation zone includes a reboiler section, maintained at a temperature within the range from about 65°

to about 110°

C.

17. The refrigeration system of claim 14 wherein an external refrigeration fluid is continuously cooled, by indirect heat exchange with the refrigerant component from the evaporation zone, to a temperature within the range from about -8°

to about +20°

C.

18. The refrigeration system of claim 16 wherein the reboiler section of the fractionation zone is continuously warmed by indirect exchange with an external source of heat.

19. The refrigeration system of claim 10 wherein the higher-boiling compound is selected from the class consisting of ethylene glycol;

diethylene glycol;

1,3-propylene glycol;

1,2-propylene glycol;

butyrolactone;

dimethyl formamide;

monoethanolamine; and

mixtures thereof.

20. The refrigeration system of claim 10 wherein the lower-boiling compound is selected from the class consisting of water;

methanol;

acetone; and

mixtures thereof.

21. The refrigeration system of claim 19 wherein the higher-boiling compound is ethylene glycol.

22. The refrigeration system of claim 20 wherein the lower-boiling compound is water.

23. The refrigeration system of claim 10 wherein the higher-boiling compound is ethylene glycol and the lower-boiling compound is water.

24. The refrigeration system of claim 10 wherein the fractionation zone comprises, in serial arrangement, a first fractionator, operating at a third, highest sub-atmospheric pressure, and a second fractionator, operating at the second, higher sub-atmospheric pressure, an overhead stream from the first fractionator providing, by indirect heat exchange, the reboiler heat duty required for operation of the second fractionator.

25. The refrigeration system of claim 24 wherein the third, highest sub-atmospheric pressure is maintained within the range from about 250 to about 760 mm. mercury absolute pressure.

26. The refrigeration system of claim 24 wherein the first fractionator includes a reboiler section, maintained at a temperture within the range from about 110°

to about 150°

C. by indirect heat exchange with an external source of heat.