DESC:FIELD
The present disclosure relates to heating and refrigeration systems. More particularly, the present disclosure relates to an apparatus for selectively providing both heating and refrigeration, only refrigeration and only heating, and to a method for selectively achieving both heating and refrigeration, only heating and only refrigeration.
BACKGROUND
The background information herein below relates to the present disclosure but is not necessarily prior art.
Industries consume a huge quantity of water during production. General usage of industrial water includes processing or in the production of chemicals and products, washing, diluting, cooling, heating and the like. In the case of heating applications, generally, many industries such as the food industry, pharmaceuticals, chemicals, automobiles and the like require hot water in the range of 60°C to 90°C for operations including heating, mixing, curing, cleaning, product manufacturing and maintenance of a sterile environment. Conventional energy sources used for the generation of hot water include fuels such as natural gas, liquefied petroleum gas, oils, and solid fuels, which may be consumed directly or by the use of electricity, derived from the above-mentioned energy sources. Alternatively, hot water can be generated using solar energy, heat pumps, geothermal heating or by hot water heat recycling. However, all these processes are associated with a huge energy consumption during the heating application, in turn adding up to the overall operating cost.
Further, industries also normally require chilled water/refrigeration for various process applications such as the liquefaction of gases like oxygen, nitrogen, propane and methane; in compressed air, purification to condense water vapour from compressed air to reduce its moisture content; in oil refineries, chemical plants and petrochemical plants to maintain a low process temperature, and metallurgy industries to temper steel and cutlery.
A heat pump is ideal for industrial applications that require both heating and cooling water, wherein the same mechanical refrigeration system can be used to obtain both the effects. The heat pumps commonly used in industrial operations are based on a vapour compression or a vapour absorption cycle. The vapour compression cycle uses high-grade energy from mechanical inputs while the vapour absorption cycle uses energy input from waste heat or heat derived from solar collectors. As a result, the vapour absorption systems are gaining favour over conventional vapour compression heat pumps in industrial applications, as they use comparatively lesser energy and are environment friendly. However, the conventional vapour absorption systems can only generate hot water up to 80°C to 90°C, thus, limiting the applications of these systems in industries. Also, these systems can only be used for heating applications by passing the hot refrigerant (water) vapours directly from the high-temperature generator to the evaporator. During this operation, the vapour absorption system can only function as a hot water generator and a simultaneous refrigeration effect cannot be obtained.
In conventional types of heating-cooling systems or vapor refrigeration systems, switching between cooling operations and heating operations can be complicated and additional components like generators, pumps and chillers may be required. This adds to the initial capital investment and the operation and maintenance costs in terms of heat and electrical inputs and utilities.
Furthermore, the conventionally known systems are associated with drawbacks such as a lower cooling COP (Coefficient of Performance) in refrigeration mode, high steam pressure requirement for a double effect cycle, and a fixed ratio of cooling to heating load. The refrigeration capacity of the currently available systems is entirely incidental, and it depends upon the heating capacity. There is also difficulty in controlling refrigeration and heating loads independently.
There is, therefore, felt a need of an apparatus that alleviates the above-mentioned drawbacks of the known prior art.
OBJECTS
Some of the objects of the present disclosure, which at least one embodiment herein satisfies, are as follows:
An object of the present disclosure is to ameliorate one or more problems of the background or to at least provide a useful alternative.
An object of the present disclosure is to provide an apparatus for selectively providing both heating and refrigeration.
Another object of the present disclosure is to provide an apparatus which substantially reduces the quantity of energy utilized to obtain the heating and refrigeration simultaneously.
Yet another object of the present disclosure is to provide an apparatus which can be used to provide only heating or only refrigeration.
Still another object of the present disclosure is to provide an apparatus which can be used to provide only refrigeration.
Yet another object of the present disclosure is to provide an apparatus that has a higher Coefficient of Performance (COP) in the refrigeration mode.
Still another object of the present disclosure is to provide an apparatus that requires less steam pressure requirement for double-effect cycle.
Yet another object of the present disclosure is to provide an apparatus that is configured for a variable ratio of cooling to heating load.
Still another object of the present disclosure is to provide an apparatus in which the refrigeration capacity is independent of the heating capacity.
Yet another object of the present disclosure is to provide an apparatus in which refrigeration and heating load can be independently controlled.
Still another object of the present disclosure is to provide an apparatus for obtaining heating and refrigeration which reduces the overall initial capital investment.
Other objects and advantages of the present disclosure will be more apparent from the following description when read in conjunction with the accompanying figures, which are not intended to limit the scope of the present disclosure.
SUMMARY
The present disclosure relates to an apparatus for selectively providing both heating and refrigeration, only refrigeration and only heating, the apparatus comprising a high temperature generator, a low temperature generator, a drain heat exchanger, a condenser, a condensed refrigerant collection tank, a high pressure evaporator, a high pressure absorber, a low pressure evaporator, a low pressure absorber, a first low temperature heat exchanger, a second low temperature heat exchanger, a high temperature heat exchanger, and a heat recovery unit,
wherein
a. the high temperature generator is connected selectively to a set of equipment selected from the group consisting of the following set of equipment: (i) the high temperature heat exchanger, (ii) the heat recovery unit, (iii) the low temperature generator, and (iv) a hot water heat exchanger;
b. the low temperature generator is connected selectively to a set of equipment selected from the group consisting of the following set of equipment: (i) the high temperature heat exchanger, (ii) the second low temperature heat exchanger, (iii) the drain heat exchanger and the condenser and the high temperature generator;
c. the hot water heat exchanger is connected selectively to a set of equipment selected from the group consisting of the following set of equipment: (i) the low temperature generator, (ii) the condenser, (iii) the drain heat exchanger, and (iv) the high pressure absorber;
d. the drain heat exchanger is connected selectively to a set of equipment selected from the group consisting of the following set of equipment: (i) the low temperature generator, (ii) the hot water heat exchanger, (iii) the condenser, (iv) the low pressure absorber, and (v) the heat recovery unit;
e. the condenser is connected selectively to a set of equipment selected from the group consisting of the following set of equipment: (i) the low temperature generator (ii) the drain heat exchanger, (iii) the condensed refrigerant collection tank, (iv) the high pressure evaporator, and (v) the low pressure absorber;
f. the condensed refrigerant collection tank is connected selectively to a set of equipment selected from the group consisting of the following set of equipment: (i) the condenser, and (ii) the high pressure evaporator;
g. the high pressure evaporator is connected selectively to a set of equipment selected from the group consisting of the following set of equipment: (i) condenser, (ii) the low pressure evaporator, (iii) the condensed refrigerant collection tank, and (iv) the high pressure absorber;
h. the high pressure absorber, is connected selectively to a set of equipment selected from the group consisting of the following set of equipment: (i) the hot water heat exchanger, (ii) the high pressure evaporator, (iii) the first low temperature heat exchanger and the second low temperature heat exchanger;
i. the low pressure evaporator is connected selectively to a set of equipment selected from the group consisting of the following set of equipment: (i) the high pressure evaporator, and (ii) the low pressure absorber;
j. the low pressure absorber is connected selectively to a set of equipment selected from the group consisting of the following set of equipment: (i) the condenser, (ii) the first low temperature heat exchanger, (iii) the drain heat exchanger, and (iv) the low pressure evaporator;
k. the first low temperature heat exchanger, is connected selectively to a set of equipment selected from the group consisting of the following set of equipment: (i) the high pressure absorber, (ii) the low pressure absorber, and (iii) the second low temperature heat exchanger;
l. the second low temperature heat exchanger, is connected selectively to a set of equipment selected from the group consisting of the following set of equipment: (i) the first low temperature heat exchanger, (ii) the high temperature heat exchanger, (iii) the condenser, and (iv) the high pressure absorber, and (v) the low temperature generator;
m. the high temperature heat exchanger, is connected selectively to a set of equipment selected from the group consisting of the following set of equipment: (i) the high temperature generator, (ii) the low temperature generator, and (iii) the second low temperature heat exchanger; and
n. the heat recovery unit is connected selectively to a set of equipment selected from the group consisting of the following set of equipment: (i) the drain heat exchanger, and (ii) the high temperature generator .
In a preferred embodiment, for achieving both heating and refrigeration under the condition of high temperature heat input, the apparatus comprises:
i. the high temperature generator adapted to receive a heat input having a temperature in the range of 130oC to 220oC in the tubes of high temperature generator and a second absorbent solution, to provide a concentrated absorbent and refrigerant vapors;
ii. the high temperature heat exchanger, adapted to receive the second absorbent solution from the high temperature generator to provide a heat extracted second absorbent solution;
iii. the low temperature generator adapted to receive heat extracted second absorbent solution from the high temperature heat exchanger and refrigerant vapors in the tubes of low temperature generator from the high temperature generator to provide a third absorbent solution, refrigerant condensate and vapors;
iv. the second low temperature heat exchanger (18), adapted to receive the third absorbent solution from the low temperature generator, to provide cooled third absorbent solution;
v. the high pressure absorber (6), adapted to receive cooled third absorbent solution from second low temperature heat exchanger (18), and water from plant having a temperature in the range of 60oC to 75oC in the tubes of high pressure absorber, to provide fourth absorbent solution which is fed to the first low temperature heat exchanger (16);
vi. the first low temperature heat exchanger (16), adapted to receive fourth absorbent solution from the high pressure absorber (6), further cooled before to the low pressure absorber (7);
vii. the low pressure absorber (7) adapted to receive cooled fourth absorbent solution from first low temperature heat exchanger (16), and water from the plant in the tubes of low pressure absorber (24), to provide first absorbent solution which is fed high temperature generator;
viii. the drain heat exchanger adapted to receive first absorbent solution from the low pressure absorber and condensed refrigerant from the tubes of low temperature generator (5) and hot water heat exchanger, to provide cooled refrigerant to condenser and hot first absorbent solution to heat recovery unit;
ix. the heat recovery unit adapted to receive hot first absorbent solution from drain heat exchanger, to further heat the hot first absorbent solution;
x. the hot water heat exchanger adapted to receive refrigerant vapors from the high temperature generator and hot water having a temperature in the range of 70 to 85°C in the tubes of hot water heat exchanger (23) from high pressure absorber, to provide condensed refrigerant and hot water to the plant;
xi. the condenser adapted to receive refrigerant vapors from low temperature generator (14) and condensed refrigerant from the drain heat exchanger, and to provide condensed refrigerant to refrigerant collection tank;
xii. the condensed refrigerant collection tank adapted to receive condensed refrigerant from the condenser, to provide the condensed refrigerant to the high pressure evaporator;
xiii. the high pressure evaporator adapted to receive condensed refrigerant from the condensed refrigerant collection tank, and water having a temperature in the range of 35 to 45°C in the tubes of high pressure evaporator (4) from the condenser, to provide, water at a temperature 30 to 40°C to the plant and adsorbent refrigerant mixture to the low-pressure evaporator;
xiv. the low pressure evaporator adapted to receive water at a temperature in the range of 10oC to 15oC in the tubes of low pressure evaporator (1) from the plant, to provide cold water to the plant.
In a preferred embodiment, the heat input is at least one selected from steam and superheated water.
In a preferred embodiment, the heat input has a pressure in the range of 6 bar to 9 bar (g).
In a preferred embodiment, the heat input at the outlet of HR (20) has a temperature in the range of 80oC to 99oC.
In a preferred embodiment, the COND (12) is operated at a pressure in the range of 35 mmHg to 50 mmHg.
In a preferred embodiment, the hot water in HWHE (23) has a temperature in the range of 60oC to 98oC.
In a preferred embodiment, the pressure in the shell (8) comprising the ABSH (6) and the EVAH (3) is in the range of 30 mmHg to 35 mmHg.
In a preferred embodiment, the water at the outlet of the EVAH (3) has a temperature in the range of 30oC to 40oC.
In a preferred embodiment, the pressure in the shell (9) comprising the ABSL (7) and the EVAL (2) is in the range of 30 mmHg to 35 mmHg.
In a preferred embodiment, the cooling water pumped using pumping means (10) to the T-ABSL (24) has a temperature in the range of 25°C to 35°C.
The present disclosure also relates to a method for achieving both heating and refrigeration, only refrigeration, and only heating, under the condition selected from a group of conditions consisting of high temperature heat input and low temperature heat input, the method comprising the following steps:
a. feeding a first adsorbent solution comprising a refrigerant and an absorbent to a high temperature generator, and heating by a heat input having temperature in the range of 130°C to 220°C, to obtain refrigerant vapours and second absorbent solution;
b. transferring the obtained second absorbent solution to the high temperature heat exchanger for exchanging the heat with the first absorbent solution coming from a second low temperature heat exchanger, and further transferring the second absorbent solution from the high temperature heat exchanger to the low temperature generator ;
c. separately, transferring the refrigerant vapours obtained in step (a) to tubes of a low temperature generator and hot water heat exchanger, and condensing the refrigerant vapors in hot water heat exchanger to obtain a condensed refrigerant;
d. heating the second absorbent solution in low temperature generator by the refrigerant vapours received from a high temperature generator to obtain a third absorbent solution, and simultaneously condensing the refrigerant vapours to obtain condensed refrigerant;
e. transferring the third absorbent solution obtained in step (d) to a second low temperature heat exchanger and further to high pressure absorber;
f. separately, combining the condensed refrigerant obtained in step (d) with the condensed refrigerant obtained from a hot water heat exchanger in step (c) and transferring to drain heat exchanger, and further to a condenser;
g. transferring the condensed refrigerant from the condenser to a high pressure evaporator and evaporating the condensed refrigerant to form refrigerant vapours and a condensed refrigerant stream, and recirculating the obtained condensed refrigerant stream to the high pressure evaporator and a low pressure evaporator;
h. evaporating the condensed refrigerant stream in the low pressure evaporator to obtain form refrigerant vapours and a condensed refrigerant stream, and recirculating the obtained condensed refrigerant stream to high pressure evaporator and low pressure evaporator;
i. contacting the obtained refrigerant vapours with the third absorbent solution in the high pressure absorber to obtain a fourth absorbent solution;
j. transferring the obtained fourth absorbent solution to first low temperature heat exchanger for heat exchange with the first absorbent solution, and further feeding to the low pressure absorber for absorbing the refrigerant vapours obtained in step (h) to obtain a first absorbent solution;
k. transferring the obtained first absorbent solution to first low temperature heat exchanger, drain heat exchanger, second low temperature heat exchanger and high temperature heat exchanger and further feeding to high temperature generator; and
l. repeating steps (a) to (k).
In a preferred embodiment, the heat input is at least one selected from steam and superheated water, and the heat input has a pressure in the range of 6 bar to 9 bar(g).
In a preferred embodiment, the heat input at the outlet of HR (20) has a temperature in the range of 80oC to 99oC, the hot water at high pressure absorber outlet has a temperature in the range of 70°C to 85oC, the hot water in HWHE (23) has a temperature in the range of 60oC to 98oC, the water at the outlet of the EVAH (3) has a temperature in the range of 30oC to 40oC, the cooling water pumped using pumping means (10) to the T-ABSL (24) has a temperature in the range of 25°C to 35°C.
In a preferred embodiment, the COND (12) is operated at a pressure in the range of 40 mmHg to 50 mmHg, the pressure in the shell (8) comprising the ABSH (6) and the EVAH (3) is in the range of 30 mmHg to 35 mmHg, and the pressure in the shell (9) comprising the ABSL (7) and the EVAL (2) is in the range of 30 mmHg to 35 mmHg.
BRIEF DESCRIPTION OF THE ACCOMPANYING DRAWINGS
An apparatus for selectively providing both heating and refrigeration, only refrigeration and only heating of the present disclosure will now be described with the help of the accompanying drawing, in which:
Figure 1 illustrates a schematic representation of an apparatus for providing heating and refrigeration using a double-effect vapour absorption cycle, in accordance with an embodiment of the present disclosure.
LIST OF REFERENCE NUMERALS USED IN DETAILED DESCRIPTION AND DRAWING
1000 Apparatus for providing heating and refrigeration using a double-effect vapour absorption cycle, in accordance with an embodiment of the present disclosure
1 heat exchanger tubes of low-pressure evaporator (EVAL)
2 low-pressure evaporator (EVAL)
3 high-pressure evaporator (EVAH)
4 tubes of high-pressure evaporator (T-EVAH)
5 tubes of high-pressure absorber (T-ABSH)
6 high-pressure absorber (ABSH)
7 low-pressure absorber (ABSL)
8 shell comprising the high-pressure absorber (ABSH) and the high-pressure evaporator (EVAH)
9 shell comprising the low-pressure absorber (ABSL) and the low-pressure evaporator (EVAL)
10 a plurality of pumping means
11 condensed refrigerant collection tank
12 condenser (COND)
13 hot-water heat exchanger (HWHE)
14 low temperature generator (LTG)
15 tubes of the low temperature generator (T-LTG)
16 first low temperature heat exchanger (LTHE1)
17 drain heat exchanger (DHE)
18 second low temperature heat exchanger (LTHE2)
19 high temperature heat exchanger (HTHE)
20 heat recovery unit (HR)
21 high temperature generator (HTG)
22 tubes of high temperature generator (T-HTG)
23 tubes of hot-water heat exchanger (T-HWHE)
24 tubes of low-pressure absorber (T-ABSL)
25 tubes of condenser (T-COND)
DETAILED DESCRIPTION
The present disclosure relates to apparatus for heating, refrigeration and a method thereof.
Embodiments of the present disclosure will now be described with reference to the accompanying drawing.
Embodiments are provided so as to thoroughly and fully convey the scope of the present disclosure to the person skilled in the art. Numerous details are set forth, relating to specific components, and methods, to provide a complete understanding of embodiments of the present disclosure. It will be apparent to the person skilled in the art that the details provided in the embodiments should not be construed to limit the scope of the present disclosure. In some embodiments, well-known processes, well-known apparatus structures, and well-known techniques are not described in detail.
The terminology used, in the present disclosure, is only for the purpose of explaining a particular embodiment and such terminology shall not be considered to limit the scope of the present disclosure. As used in the present disclosure, the forms "a,” "an," and "the" may be intended to include the plural forms as well, unless the context clearly suggests otherwise. The terms "comprises," "comprising," “including,” and “having,” are open ended transitional phrases and therefore specify the presence of stated features, integers, steps, operations, elements, modules, units and/or components, but do not forbid the presence or addition of one or more other features, integers, steps, operations, elements, components, and/or groups thereof. The particular order of steps disclosed in the method and process of the present disclosure is not to be construed as necessarily requiring their performance as described or illustrated. It is also to be understood that additional or alternative steps may be employed.
As used herein, the term "and/or" includes any and all combinations of one or more of the associated listed elements.
The terms first, second, third, etc., should not be construed to limit the scope of the present disclosure as the aforementioned terms may be only used to distinguish one element, component, region, layer or section from another component, region, layer or section. Terms such as first, second, third etc., when used herein do not imply a specific sequence or order unless clearly suggested by the present disclosure.
When an element is referred to as being “mounted on”, “engaged to”, “connected to” or “coupled to” another element, it may be directly on, engaged, connected or coupled to the other element. As used herein, the term “and/or” includes any and all combinations of one or more of the associated listed elements.
Terms such as “inner”, “outer”, “beneath”, “below”, “lower”, “above”, “upper” and the like, may be used in the present disclosure to describe relationships between different elements as depicted from the figures.
The conventionally known chiller heat pump systems are associated with drawbacks such as a lower cooling COP (Coefficient of Performance) in refrigeration mode, high steam pressure requirement for double effect cycle, a fixed ratio of cooling to heating load. The refrigeration capacity of the currently available systems is entirely depends upon the heating capacity. There is also difficulty in controlling refrigeration and heating loads independently.
To avoid the shortcomings of the conventional chiller heat pump, the present disclosure envisages an apparatus (hereinafter referred to as ‘apparatus 1000’) that offers advantages such as a higher COP (Coefficient of Performance) in refrigeration mode, lower steam pressure requirement for double effect cycle and alleviates the drawbacks of the apparatus in the prior art.
The present disclosure provides an apparatus for selectively providing both heating and refrigeration, only refrigeration and only heating, and a method for selectively achieving both heating and refrigeration, only heating and only refrigeration.
In an aspect, the present disclosure provides to an apparatus for selectively providing both heating and refrigeration, only refrigeration and only heating.
In accordance with an embodiment of the present disclosure, the apparatus comprises a low-pressure evaporator (EVAL), a high-pressure evaporator (EVAH), a low-pressure absorber (ABSL), a high-pressure absorber (ABSH), condenser (COND), a low temperature generator (LTG), a high temperature generator (HTG), a first low temperature heat exchanger (LTHE1), a second low temperature heat exchanger (LTHE2) and a heat recovery unit (HR), further comprising a drain heat exchanger (DHE) and a high temperature heat exchanger (HTHE) and hot-water heat exchanger (HWHE). The apparatus is configured to selectively providing both heating and refrigeration, only refrigeration and only heating using a double-effect vapour absorption cycle, under the conditions of high temperature heat input, wherein the refrigerant-absorbent mixture used in the apparatus of the present disclosure includes, but is not limited to water- lithium bromide, ammonia-water. Any other suitable refrigerant-absorbent mixture can be used.
In accordance with an embodiment of the present disclosure, the apparatus for selectively providing both heating and refrigeration, only refrigeration and only heating, is provided. The apparatus comprising a high temperature generator (21), a low temperature generator (14), a drain heat exchanger (17), a condenser (12), a condensed refrigerant collection tank (11), a high pressure evaporator (3), a high pressure absorber (6), a low pressure evaporator (2), a low pressure absorber (7), a first low temperature heat exchanger (16), a second low temperature heat exchanger (18), a high temperature heat exchanger (19), and a heat recovery unit (20).
The high temperature generator (21) is connected selectively to a set of equipment selected from the group consisting of the following set of equipment: (i) the high temperature heat exchanger (19), (ii) the heat recovery unit (20), (iii) the low temperature generator (14), and (iv) to a hot water heat exchanger (13).
The low temperature generator (14) is connected selectively to a set of equipment selected from the group consisting of the following set of equipment: (i) the high temperature heat exchanger (19), (ii) the second low temperature heat exchanger (18), (iii) the drain heat exchanger (17) and the condenser (12) and the high temperature generator (21).
The hot water heat exchanger (13) is connected selectively to a set of equipment selected from the group consisting of the following set of equipment: (i) the low temperature generator (14), (ii) the condenser (12), (iii) the drain heat exchanger (17), and (iv) the high pressure absorber (6).
The drain heat exchanger (17) is connected selectively to a set of equipment selected from the group consisting of the following set of equipment: (i) the low temperature generator (14), (ii) the hot water heat exchanger (13), (iii) the condenser (12), (iv) the low pressure absorber (7), and (v) the heat recovery unit (20).
The condenser (12) is connected selectively to a set of equipment selected from the group consisting of the following set of equipment: (i) the low temperature generator (14), (ii) the drain heat exchanger (17), (iii) the condensed refrigerant collection tank (11), (iv) the high pressure evaporator (3), and (v) the low pressure absorber (7).
The condensed refrigerant collection tank (11) is connected selectively to a set of equipment set of equipment set of equipment selected from the group consisting of the following set of equipment: (i) the condenser (12), and (ii) the high pressure evaporator (3).
The high pressure evaporator (3) is connected selectively to a set of equipment selected from the group consisting of the following set of equipment: (i) condenser (12), (ii) the low pressure evaporator (2), (iii) the condensed refrigerant collection tank (11), and (iv) the high pressure absorber (6).
The high pressure absorber (6), is connected selectively to a set of equipment selected from the group consisting of the following set of equipment: (i) the hot water heat exchanger (13), (ii) the high pressure evaporator (3), (iii) the first low temperature heat exchanger (16) and the second low temperature heat exchanger (18).
The low pressure evaporator (2) is connected selectively to a set of equipment selected from the group consisting of the following set of equipment: (i) the high pressure evaporator (3), and (ii) the low pressure absorber (7).
The low pressure absorber (7) is connected selectively to a set of equipment selected from the group consisting of the following set of equipment: (i) the condenser (12), (ii) the first low temperature heat exchanger (16), (iii) the drain heat exchanger (17), and (iv) the low pressure evaporator (2).
The first low temperature heat exchanger (16), is connected selectively to a set of equipment selected from the group consisting of the following set of equipment: (i) the high pressure absorber (6), (ii) the low pressure absorber (7), and (iii) the second low temperature heat exchanger (18).
The second low temperature heat exchanger (18), is connected selectively to a set of equipment selected from the group consisting of the following set of equipment: (i) the first low temperature heat exchanger (16), (ii) the high temperature heat exchanger (19), (iii) the condenser (12), (iv) the high pressure absorber (6), and (v) the low temperature generator (14).
The high temperature heat exchanger (19), is connected selectively to a set of equipment selected from the group consisting of the following set of equipment: (i) the high temperature generator (21), (ii) the low temperature generator (14), and (iii) the second low temperature heat exchanger (18).
The heat recovery unit (20) is connected selectively to a set of equipment selected from the group consisting of the following set of equipment: (i) the drain heat exchanger (17), and (ii) the high temperature generator (21).
In an embodiment of the present disclosure, a plurality of pumping means (10) are used for pumping the desired fluid to the desired stage.
An apparatus (1000), of the present disclosure will now be described with reference to Figure 1. Figure 1 illustrates a schematic diagram of an apparatus for providing both heating and refrigeration using a double-effect vapour absorption cycle for a refrigerant-absorbent mixture under the condition of high temperature heat input, in accordance with an embodiment of the present disclosure.
The preferred embodiment does not limit the scope and ambit of the present disclosure.
The apparatus illustrated in the figure 1, the refrigerant-absorbent mixture, typically Li-Br and water, first enters the high temperature generator (21) and hot water first enters the ABSH (6) and then HWHE (13).
The embodiment as disclosed in the figure 1, comprises feeding a first absorbent solution from the HTHE (19) and HR (20) to HTG (21). The first absorbent solution from the HTHE (19) and HR (20) are mixed together and sent to the HTG (21). The first absorbent solution comprises an absorbent and a refrigerant.
The HTG (21) is provided with a high temperature heat input having temperature in the range of 130°C to 220°C, which boils refrigerant in the first absorbent solution entering the HTG (21) to obtain a second absorbent solution. The obtained second absorbent solution is more concentrated than the first absorbent solution. In an embodiment of the present disclosure, the second absorbent solution has a temperature in the range of 150oC to 160oC. In accordance with the embodiments of the present disclosure, the heat input used in the HTG (21) can include, but is not limited to, steam, superheated water, obtained by combustion of fuel or exhaust gas. Other known suitable heat inputs can also be used. In an embodiment of the present disclosure, the heat input is a steam having a pressure in the range of 6 bar to 9 bar(g). After extracting heat from the heat input in the HTG (21), the remaining heat is reclaimed in the HR (20), which is provided to reclaim optimum quantity of heat input in the double-effect vapour absorption cycle and utilize it to enhance the heating effect thus provided. In an embodiment of the present disclosure, the heat input at the outlet of HR (20) has a temperature in the range of 80oC to 99oC.
The second absorbent solution from the HTG (21) is sent to the HTHE (19) for exchanging the heat with the first absorbent solution coming from LTHE2 (18). The second absorbent solution from the HTHE (19) is fed to the LTG (14).
The refrigerant vapours generated from the HTG (21) are bifurcated into a first stream and a second stream. The first stream is fed to T-LTG (15) and the second stream is fed to HWHE (13). The partial refrigerant vapours after leaving the HTG (21) are sent through the heat exchanger tubes of the T-LTG (15). The vapours act as a further heating source for the second absorbent solution, thus concentrating it further to obtain a third absorbent solution, simultaneously, the refrigerant vapours get condensed. The third absorbent solution, thus obtained in the LTG (14) is the most concentrated absorbent solution achieved using the present process cycle.
Thereafter, the third absorbent solution is sent to the LTHE2 (18), where the heat is gained by the first absorbent solution coming from LTHE1 (16). The third absorbent solution stream leaving the LTHE2 (18) is fed to the ABSH (6).
The partial refrigerant vapours generated from HTG (21) are passed through the T-LTG (15) and used as a heat source to generate refrigerant vapours in the LTG (14). The refrigerant vapours generated in the LTG (14) are sent to the COND (12), wherein the refrigerant vapours are condensed by exchanging heat with cooling water coming from the T-ABSL (24). After exchanging the heat in the T-LTG (15), the refrigerant vapours generated from the HTG (21) are condensed in the tubes T-LTG (15).
The remaining refrigerant vapours generated from the HTG (21) are fed to HWHE (13) and are used to exchange the heat with hot water in HWHE (23), coming from ABSH (5). In an embodiment of the present disclosure, the hot water in HWHE (23) has a temperature in the range of 85oC to 98oC. The refrigerant condensate from both the T-LTG (15) and the HWHE (13) are mixed and pass through DHE (17), where the refrigerant condensate exchanges heat with the first absorbent solution and is then fed to COND (12). In the COND (12), the refrigerant condensate is further condensed and is collected in the condensed refrigerant collection tank (11).
In Figure 1, numeral (8) represents a shell comprising the ABSH (6) and the EVAH (3). By maintaining a high-pressure in the ABSH (6) and the EVAH (3) in the shell (8), the condensed refrigerant is vaporized. The tubes of high-pressure evaporator-T-EVAH (4) are provided with water. During the cycle, water exchanges heat in the EVAH (3), with the condensed refrigerant coming from the COND (12), i.e. from the condensed refrigerant collection tank (11). In an embodiment of the present disclosure, water at the outlet of the EVAH (3) has a temperature in the range of 30oC to 40oC. The condensed refrigerant stream leaving the EVAH (3) is recycled back to the EVAH (3) via the pumping means (10). The condensed refrigerant extracts heat from water circulating through the evaporator tubes EVAH (4) and forms refrigerant vapours. The refrigerant vapours thus released in the EVAH (3), are absorbed by the concentrated third absorbent solution fed to the ABSH (6). The concentrated third absorbent solution absorbs the refrigerant vapours in the ABSH (6), to obtain a fourth absorbent solution and gets collected in the sump. The fourth absorbent solution is more dilute in comparison with the third absorbent solution. Heat is liberated during the refrigerant vapour absorption process, referred to as the heat of dilution. Hot water, having a temperature in the range of 55°C to 70°C, is pumped by pumping means (10) through the T-ABSH (5), wherein the hot water gains the heat of dilution produced during the refrigerant vapour absorption process. In an embodiment of the present disclosure, a plurality of pumping means (10) are used. The hot water leaving the T-ABSH (5) is fed to T-HWHE (23), which extracts the heat from refrigerant vapours coming from HTG (21). Thus, the hot water temperature is increased to a temperature in the range of 60°C to 98°C and is used for heating applications. In another embodiment, the hot water temperature is increased to a temperature in the range of 85 °C to 95 °C.
The fourth absorbent solution collected in ABSH (6) sump, is pumped using pumping means (10) to the ABSL (7) through the LTHE (1). The fourth absorbent solution rejects its heat to the first absorbent solution in the LTHE and gets cool down before it enters to the ABSL (7). This heat exchange process helps to reduce the vapour flash loss in the ABSL (7).
In Figure 1, numeral (9) represents a shell comprising the ABSL (7) and the EVAL (2). The fourth absorbent solution, after losing heat in the LTHE1 (16) is fed to the ABSL (7). By maintaining a low-pressure in the ABSL (7) and the EVAL (2) in the shell 9, the condensed refrigerant vaporizes at a low temperature. The condensed refrigerant stream leaving the EVAL (2) is recycled back to the EVAL (2) via the pumping means (10). The EVAL (2) is fed with water having a temperature in the range of 10 °C to 15 °C through the heat exchanger tubes EVAL (1). The vaporizing causes the condensed refrigerant to extract heat from the water circulated through the tubes of the EVAL (1), thus producing refrigerant vapours and cooling the water circulated therein up to a temperature in the range of 5°C to 10°C. The refrigerant vapours produced in the EVAL (2) are absorbed by the fourth absorbent solution fed to the ABSL (7). The fourth absorbent solution, after absorbing the refrigerant vapours gets diluted to obtain first absorbent and gets collected in the sump. Thus, the first absorbent solution is more dilute in comparison with the fourth absorbent solution. The process of refrigerant absorption produces heat of dilution, which is absorbed by the water circulated through the T-ABSL (24). This cooling water is pumped using pumping means (10) to the T-ABSL (24) through the tubes. In an embodiment of the present disclosure, the cooling water pumped using pumping means (10) to the T-ABSL (24) has a temperature in the range of 25°C to 35°C. The water gains heat in the T-ABSL (24), and is fed to the T-COND (25), wherein it extracts the heat of condensation and is then fed to T-EVAH (4), wherein it loses the heat.
The first absorbent solution is collected in the sump of the ABSL (7). This first absorbent solution is pumped by pumping means (10) to the HTG (21). The pumped first absorbent solution is bifurcated into a first and a second stream, and passed through the set of heat exchangers, and is then fed to the HTG (21). The first stream is fed to the LTHE1 (16) and the second stream is fed to DHE (17). The first absorbent solution extracts heat in the LTHE1 (16) from the fourth absorbent solution coming from ABSH (6). From the LTHE1 (16), the first absorbent solution is fed to the LTHE2 (18), wherein the first absorbent solution further extracts heat from the third absorbent solution fed to the LTHE2 (18) from the LTG (14). This step helps in reducing the temperature of the third absorbent solution from the LTG (14) before feeding it to the absorber ABSH (6). In the DHE (17), the remaining first absorbent solution extracts heat from the refrigerant condensate coming from the T-LTG (15) and HWHE (13), wherein the temperature of the first absorbent solution increases, and the refrigerant condensate is suitably cooled before feeding to the COND (12).
The heated first absorbent solution leaving the LTHE2 (18) is fed to the HTHE (19) and the first absorbent solution leaving DHE (17) is fed to the HR (20). In the HTHE (19), the first absorbent solution extracts heat from the second absorbent solution leaving the HTG (21). In the HR (20), the first absorbent solution gets heated up by extracting the heat from the steam condensate. The steam condensate is cooled down before discharging to the condensate tank. The first absorbent solution after gaining heat in the HTHE (19) is mixed with the absorbent solution coming from the HR (20), and fed to the HTG (21), where the first absorbent solution is boiled, and refrigerant vapours are generated. The second absorbent solution from HTHE (19), is fed to the LTG (14) after exchanging heat with the first absorbent solution.
In accordance with the embodiments of the present disclosure, the second absorbent solution has a temperature in the range of 150oC to 160oC.
In accordance with the embodiments of the present disclosure, the heat input used in the HTG (21) can include, but is not limited to, steam, superheated water, obtained by combustion of fuel or exhaust gas. In an embodiment of the present disclosure, the heat input is a steam having a pressure in the range of 6 bar to 9 bar(g).
In accordance with the embodiments of the present disclosure, the heat input at the outlet of HR (20) has a temperature in the range of 80oC to 99oC.
In accordance with the embodiments of the present disclosure, the third absorbent solution has a temperature in the range of 88oC to 95oC.
In accordance with the embodiments of the present disclosure, the hot water in HWHE (23) has a temperature in the range of 85oC to 98oC.
In accordance with the embodiments of the present disclosure, in the COND (12), the refrigerant condensate is further condensed and is collected in the condensed refrigerant collection tank (11).
In accordance with the embodiments of the present disclosure, water at the outlet of the EVAH (3) has a temperature in the range of 30oC to 40oC.
In accordance with the embodiments of the present disclosure, the water fed to the EVAL (2) has a temperature in the range of 10°C to 15°C.
In accordance with the embodiments of the present disclosure, the water from the outlet of the EVAL (2) has a temperature in the range of 5°C to 10°C.
In accordance with the embodiments of the present disclosure, the the cooling water pumped using pumping means (10) to the T-ABSL (24) has a temperature in the range of 30°C to 35°C.
In accordance with the embodiments of the present disclosure, the hot water heat exchanger (13) is recovers the heat from refrigerant vapours generated by the HTG (21). Thus, a high temperature heat source such as steam received in tube (22) can be modulated using control valve and vary the heating load of the heat exchanger (13), which in turn avoids the system of having fixed cooling to heating load ratio.
In accordance with the embodiments of the present disclosure, the flow of hot water through both the high pressure absorber ABSH (5) and the hot water heat exchanger HWHE (13) in series, thus, a variable cooling to heating load is achieved.
Furthermore, the conventional apparatus has a cooling coefficient of performance (COP) is in the range of 0.25 to 0.35. On the contrary, the apparatus f the present disclosure has a cooling coefficient of performance (COP) in the range of 1.4 to 1.5. Thus, the cooling coefficient of performance (COP) is enhanced to a large extent by using the apparatus of the present disclosure.
In the conventional apparatus, the water getting generated from the condenser is coupled with the single effect generator requires a high steam pressure of about 6 bar to 9 bar(g). Further, if there is one more generator in the conventional apparatus, for making double effect cycle, then steam pressure required will be increased to about 20 to 25 bar(g). Contrarily, in the apparatus of the present disclosure, hot water is getting generated using the hot water heat exchanger HWHE (13), which is recovering heat from the refrigerant vapours received from the HTG (21), and therefore, the steam pressure required in the double effect cycle is low. In an embodiment, the steam pressure required is 6 bar to 9 bar(g).
In accordance with the embodiments of the present disclosure, in the apparatus, the refrigeration capacity is entirely incidental, and it depends upon the heating capacity due to variable ratio of cooling to heating load. Therefore, in the apparatus of the present disclosure, the refrigerant capacity does not depend upon the heating capacity. On the contrary, in the conventionally used apparatus, due to fixed ratio of cooling to heating load, refrigeration capacity produced depends upon the heating capacity.
In the conventional apparatus, the heating capacity only can be controlled, and refrigeration capacity is incidental with respect to the heating capacity, and therefore, there is a difficulty in controlling refrigeration and heating loads independently. However, in the apparatus of the present disclosure, both the heating and the refrigeration capacities can be varied with respect to the requirement.
Thus, in the apparatus of the present disclosure, the heat from refrigerant vapour is picked up for heating from two different heat exchangers, Absorber and Hot water heat exchanger. This solves the problem of having fixed cooling load for the specified heating load. Further, there is no requirement of an inter-circulation pump, as conventionally used. The requirement of flash heat exchanger is obviated, thus considerably increasing the coefficient of performance. Furthermore, the boiling temperature of the absorbent solution in the high temperature generator is very low in comparison with the conventional apparatus, thus the apparatus of the present disclosure requires less steam pressure / heat inlet temperature.
In another aspect, the present disclosure provides a method for providing both heating and refrigeration using a double-effect vapour absorption cycle in an apparatus (1000).
The method includes the following steps:
a. feeding a first adsorbent solution comprising a refrigerant and an absorbent to a high temperature generator (21), and heating by a heat input having temperature in the range of 130°C to 220°C, to obtain refrigerant vapours and second absorbent solution;
b. transferring the obtained second absorbent solution to a high temperature heat exchanger (19) for exchanging the heat with the first absorbent solution coming from a second low temperature heat exchanger (18), and further transferring the second absorbent solution from the high temperature heat exchanger (19) to a low temperature generator (14);
c. separately, transferring the refrigerant vapours obtained in step (a) to tubes of a low temperature generator (15) and a hot water heat exchanger (13), and condensing the refrigerant vapors in a hot water heat exchanger (13) to obtain a condensed refrigerant;
d. heating the second absorbent solution in the low temperature generator (14) by the refrigerant vapours received from the high temperature generator (21) to obtain a third absorbent solution, and simultaneously condensing the refrigerant vapours to obtain condensed refrigerant;
e. transferring the third absorbent solution obtained in step (d) to a second low temperature heat exchanger (18) and further to a high pressure absorber (6);
f. separately, combining the condensed refrigerant obtained in step (d) with the condensed refrigerant obtained from hot water heat exchanger (13) in step (c) and transferring to a drain heat exchanger (17), and further to a condenser (12);
g. transferring the condensed refrigerant from condenser (12) to a high pressure evaporator (3) and evaporating the condensed refrigerant to form refrigerant vapours and a condensed refrigerant stream, and recirculating the obtained condensed refrigerant stream to the high pressure evaporator (3) and a low pressure evaporator (2);
h. evaporating the condensed refrigerant stream in the low pressure evaporator (2) to obtain form refrigerant vapours and a condensed refrigerant stream, and recirculating the obtained condensed refrigerant stream to the high pressure evaporator (3) and the low pressure evaporator (2);
i. contacting the obtained refrigerant vapours with the third absorbent solution in the high pressure absorber (6) to obtain a fourth absorbent solution;
j. transferring the obtained fourth absorbent solution to first low temperature heat exchanger for heat exchange with the first absorbent solution, and further feeding to the low pressure absorber (7) for absorbing the refrigerant vapours obtained in step (h) to obtain a first absorbent solution;
k. transferring the obtained first absorbent solution to the first low temperature heat exchanger (16), the drain heat exchanger (17), the second low temperature heat exchanger (18) and the high temperature heat exchanger (19) and further feeding to the high temperature generator (21); and
l. repeating steps (a) to (k).
In accordance with the embodiments of the present disclosure, the second absorbent solution has a temperature in the range of 150oC to 160oC.
In accordance with the embodiments of the present disclosure, the heat input used in the HTG (21) can include, but is not limited to, steam, and superheated water, obtained by the combustion of fuel or exhaust gas. In an embodiment of the present disclosure, the heat input is a steam having a pressure in the range of 6 bar to 9 bar(g).
In accordance with the embodiments of the present disclosure, the heat input at the outlet of HR (20) has a temperature in the range of 80oC to 99oC.
In accordance with the embodiments of the present disclosure, the third absorbent solution has a temperature in the range of 88oC to 95oC.
In accordance with the embodiments of the present disclosure, the hot water in HWHE (23) has a temperature in the range of 85oC to 98oC.
In accordance with the embodiments of the present disclosure, in the COND (12), the refrigerant condensate is further condensed and is collected in the condensed refrigerant collection tank (11).
In accordance with the embodiments of the present disclosure, water at the outlet of the EVAH (3) has a temperature in the range of 30oC to 40oC.
In accordance with the embodiments of the present disclosure, the water fed to the EVAL (2) has a temperature in the range of 10°C to 15°C.
In accordance with the embodiments of the present disclosure, the water from the outlet of the EVAL (2) has a temperature in the range of 5°C to 10°C.
In accordance with the embodiments of the present disclosure, the the cooling water pumped using pumping means (10) to the T-ABSL (24) has a temperature in the range of 25°C to 35°C.
The foregoing description of the embodiments has been provided for purposes of illustration and not intended to limit the scope of the present disclosure. Individual components of a particular embodiment are generally not limited to that particular embodiment but are interchangeable. Such variations are not to be regarded as a departure from the present disclosure, and all such modifications are considered to be within the scope of the present disclosure.
The present disclosure is further described in light of the following experiments which are set forth for illustration purpose only and not to be construed for limiting the scope of the disclosure. The following experiments can be tested to scale up to industrial/commercial scale and the results obtained can be extrapolated to the industrial scale.
TECHNICAL ADVANCEMENTS
The present disclosure described herein above has several technical advantages including, but not limited to, the realization of an apparatus for selectively providing both heating and refrigeration, only refrigeration and only heating that:
• provides a higher cooling COP (Coefficient of Performance) in refrigeration mode;
• has a lower steam pressure requirement for double-effect cycle;
• provides a flexible ratio of cooling to heating load, and independent control of refrigeration and heating loads;
• is energy efficient;
• saves fuel;
• is compact; and
• the apparatus can be operated to provide both heating and refrigeration, only heating, and only refrigeration depending upon the heat input available and the customer's requirements.
Further, the vapour absorption heat pumps substantially reduce operating costs as they use low-grade waste heat. Also, the vapour absorption systems use non-ozone-depleting refrigerants (water) and require much lesser electricity compared to the vapour compression systems. These systems are even more beneficial for industrial applications where waste heat can be used to generate steam/hot water. The technology also helps to reduce emissions, improves efficiency, and limits the use of groundwater for cooling. The apparatus is efficient in heating and cooling, thus significantly reducing energy costs.
and
a method for selectively providing both heating and refrigeration, only refrigeration and only heating, that is
• simple to perform;
• environment friendly; and
• economic.
Throughout this specification the word “comprise”, or variations such as “comprises” or “comprising”, will be understood to imply the inclusion of a stated element, integer or step, or group of elements, integers or steps, but not the exclusion of any other element, integer or step, or group of elements, integers or steps.
The use of the expression “at least” or “at least one” suggests the use of one or more elements or ingredients or quantities, as the use may be in the embodiment of the invention to achieve one or more of the desired objects or results. While certain embodiments of the inventions have been described, these embodiments have been presented by way of example only, and are not intended to limit the scope of the inventions. Variations or modifications to the formulation of this invention, within the scope of the invention, may occur to those skilled in the art upon reviewing the disclosure herein. Such variations or modifications are well within the spirit of this invention.
The numerical values given for various physical parameters, dimensions and quantities are only approximate values and it is envisaged that the values higher than the numerical value assigned to the physical parameters, dimensions and quantities fall within the scope of the invention unless there is a statement in the specification to the contrary.
While considerable emphasis has been placed herein on the specific features of the preferred embodiment, it will be appreciated that many additional features can be added and that many changes can be made in the preferred embodiment without departing from the principles of the disclosure. These and other changes in the preferred embodiment of the disclosure will be apparent to those skilled in the art from the disclosure herein, whereby it is to be distinctly understood that the foregoing descriptive matter is to be interpreted merely as illustrative of the disclosure and not as a limitation. ,CLAIMS:WE CLAIM:
1. An apparatus for selectively providing both heating and refrigeration, only refrigeration and only heating, said apparatus comprising a high temperature generator (21), a low temperature generator (14), a drain heat exchanger (17), a condenser (12), a condensed refrigerant collection tank (11), a high pressure evaporator (3), a high pressure absorber (6), a low pressure evaporator (2), a low pressure absorber (7), a first low temperature heat exchanger (16), a second low temperature heat exchanger (18), a high temperature heat exchanger (19), and a heat recovery unit (20),
wherein
a. said high temperature generator (21) is connected selectively to a set of equipment selected from the group consisting of the following set of equipment: (i) said high temperature heat exchanger (19), (ii) said heat recovery unit (20), (iii) said low temperature generator (14), and (iv) to a hot water heat exchanger (13);
b. said low temperature generator (14) is connected selectively to a set of equipment selected from the group consisting of the following set of equipment: (i) said high temperature heat exchanger (19), (ii) said second low temperature heat exchanger (18), (iii) said drain heat exchanger (17) and said condenser (12) and said high temperature generator (21);
c. said hot water heat exchanger (13) is connected selectively to a set of equipment selected from the group consisting of the following set of equipment: (i) said high temperature generator (21), (ii) said condenser (12), (iii) said drain heat exchanger (17), and (iv) said high pressure absorber (6);
d. said drain heat exchanger (17) is connected selectively to a set of equipment selected from the group consisting of the following set of equipment: (i) said low temperature generator (14), (ii) said hot water heat exchanger (13), (iii) said condenser (12), (iv) said low pressure absorber (7), and (v) said heat recovery unit (20);
e. said condenser (12) is connected selectively to a set of equipment selected from the group consisting of the following set of equipment: (i) said low temperature generator (14), (ii) said drain heat exchanger (17), (iii) said condensed refrigerant collection tank (11), (iv) said high pressure evaporator (3), and (v) said low pressure absorber (7);
f. said condensed refrigerant collection tank (11) is connected selectively to a set of equipment set of equipment set of equipment selected from the group consisting of the following set of equipment: (i) said condenser (12), and (ii) said high pressure evaporator (3);
g. said high pressure evaporator (3) is connected selectively to a set of equipment selected from the group consisting of the following set of equipment: (i) condenser (12), (ii) said low pressure evaporator (2), (iii) said condensed refrigerant collection tank (11), and (iv) said high pressure absorber (6);
h. said high pressure absorber (6), is connected selectively to a set of equipment selected from the group consisting of the following set of equipment: (i) said hot water heat exchanger (13), (ii) said high pressure evaporator (3), (iii) said first low temperature heat exchanger (16) and said second low temperature heat exchanger (18);
i. said low pressure evaporator (2) is connected selectively to a set of equipment selected from the group consisting of the following set of equipment: (i) said high pressure evaporator (3), and (ii) said low pressure absorber (7);
j. said low pressure absorber (7) is connected selectively to a set of equipment selected from the group consisting of the following set of equipment: (i) said condenser (12), (ii) said first low temperature heat exchanger (16), (iii) said drain heat exchanger (17), and (iv) said low pressure evaporator (2);
k. said first low temperature heat exchanger (16), is connected selectively to a set of equipment selected from the group consisting of the following set of equipment: (i) said high pressure absorber (6), (ii) said low pressure absorber (7), and (iii) said second low temperature heat exchanger (18);
l. said second low temperature heat exchanger (18), is connected selectively to a set of equipment selected from the group consisting of the following set of equipment: (i) said first low temperature heat exchanger (16), (ii) said high temperature heat exchanger (19), (iii) said condenser (12), and (iv) said high pressure absorber (6);
m. said high temperature heat exchanger (19), is connected selectively to a set of equipment selected from the group consisting of the following set of equipment: (i) said high temperature generator (21), (ii) said condenser (12), and (iii) said second low temperature heat exchanger (18); and
n. said heat recovery unit (20) is connected selectively to a set of equipment selected from the group consisting of the following set of equipment: (i) said drain heat exchanger (17), and (ii) said high temperature generator (21).
2. The apparatus as claimed in claim 1, wherein for achieving both heating and refrigeration under the condition of high temperature heat input, said apparatus comprises:
i. said high temperature generator (21) adapted to receive a heat input having a temperature in the range of 130oC to 220oC in the tubes of high temperature generator (22) and a second absorbent solution, to provide a concentrated absorbent and refrigerant vapors;
ii. said high temperature heat exchanger (19), adapted to receive the second absorbent solution from the high temperature generator (21) to provide a heat extracted second absorbent solution;
iii. said low temperature generator (14) adapted to receive heat extracted second absorbent solution from the high temperature heat exchanger (19) and refrigerant vapors in the tubes of low temperature generator (15) from the high temperature generator (21) to provide a third absorbent solution, refrigerant condensate and vapors;
iv. said second low temperature heat exchanger (18), adapted to receive the third absorbent solution from the low temperature generator (14), to provide cooled third absorbent solution;
v. said high pressure absorber (6), adapted to receive cooled third absorbent solution from second low temperature heat exchanger (18), and water from plant having a temperature in the range of 55°C to 70oC in the tubes of high pressure absorber (5), to provide fourth absorbent solution which is fed to the first low temperature heat exchanger (16);
vi. said first low temperature heat exchanger (16), adapted to receive fourth absorbent solution from the high pressure absorber (6), further cooled before providing to low pressure absorber (7);
vii. said low pressure absorber (7) adapted to receive cooled r fourth absorbent solution from first low temperature heat exchanger (16), and water from the plant in the tubes of low pressure absorber (24), to provide first absorbent solution which is fed high temperature generator (21);
viii. said drain heat exchanger (17) adapted to receive first absorbent solution from said low pressure absorber (7) and condensed refrigerant from the tubes of low temperature generator (5) and hot water heat exchanger (13), to provide cooled refrigerant to condenser (12) and hot first absorbent solution to heat recovery unit (20);
ix. said heat recovery unit (20) adapted to receive hot first absorbent solution from drain heat exchanger (17), to further heat the hot first absorbent solution;
x. said hot water heat exchanger (13) adapted to receive refrigerant vapors from the high temperature generator (21) and hot water having a temperature in the range of 70 to 85°C in the tubes of hot water heat exchanger (23) from high pressure absorber (6), to provide condensed refrigerant and hot water to the plant;
xi. said condenser (12) adapted to receive refrigerant vapors in the tubes of condenser (25) from the high temperature generator (21) and second absorbent solution from high temperature heat exchanger (19), to provide partially condensed refrigerant to the drain heat exchanger (17), and third adsorbent solution to second low temperature heat exchanger (18);
xii. said condensed refrigerant collection tank (11) adapted to receive condensed refrigerant from the condenser (12), to provide the condensed refrigerant to the high pressure evaporator (3);
xiii. said high pressure evaporator (3) adapted to receive condensed refrigerant from the condensed refrigerant collection tank (11), and water having a temperature in the range of 35 to 45°C in the tubes of high pressure evaporator (4) from the condenser (12), to provide, water at a temperature 30 to 40°C to the plant and adsorbent refrigerant mixture to the low-pressure evaporator (2);
xiv. said low pressure evaporator (2) adapted to receive water at a temperature in the range of 10oC to 15oC in the tubes of low pressure evaporator (1) from the plant, to provide cold water to the plant.
3. The apparatus as claimed in claim 2, wherein said heat input is at least one selected from steam and superheated water; and wherein said heat input has a pressure in the range of 6 bar to 9 bar(g).
4. The apparatus as claimed in claim 2, wherein the heat input at the outlet of HR (20) has a temperature in the range of 80oC to 99oC.
5. The apparatus as claimed in claim 2, wherein the third absorbent solution has a temperature in the range of 88oC to 95oC.
6. The apparatus as claimed in claim 2, wherein the hot water in HWHE (23) has a temperature in the range of 60oC to 98oC.
7. The apparatus as claimed in claim 2, wherein water at the outlet of the EVAH (3) has a temperature in the range of 30oC to 40oC.
8. The apparatus as claimed in claim 2, wherein the cooling water pumped using pumping means (10) to the T-ABSL (24) has a temperature in the range of 25°C to 35°C.
9. A method for achieving both heating and refrigeration, only refrigeration, and only heating, under the condition selected from a group of conditions consisting of high temperature heat input and low temperature heat input, said method comprising the following steps:
a. feeding a first adsorbent solution comprising a refrigerant and an absorbent to a high temperature generator (21), and heating by a heat input having temperature in the range of 130°C to 220°C, to obtain refrigerant vapours and second absorbent solution;
b. transferring the obtained second absorbent solution to a high temperature heat exchanger (19) for exchanging the heat with the first absorbent solution coming from a second low temperature heat exchanger (18), and further transferring the second absorbent solution from the high temperature heat exchanger (19) to a low temperature generator (14);
c. separately, transferring the refrigerant vapours obtained in step (a) to tubes of a low temperature generator (15) and a hot water heat exchanger (13), and condensing the refrigerant vapors in a hot water heat exchanger (13) to obtain a condensed refrigerant;
d. heating the second absorbent solution in the low temperature generator (14) by the refrigerant vapours received from the high temperature generator (21) to obtain a third absorbent solution, and simultaneously condensing the refrigerant vapours to obtain condensed refrigerant;
e. transferring the third absorbent solution obtained in step (d) to a second low temperature heat exchanger (18) and further to a high pressure absorber (6);
f. separately, combining the condensed refrigerant obtained in step (d) with the condensed refrigerant obtained from hot water heat exchanger (13) in step (c) and transferring to a drain heat exchanger (17), and further to a condenser (12);
g. transferring the condensed refrigerant from condenser (12) to a high pressure evaporator (3) and evaporating the condensed refrigerant to form refrigerant vapours and a condensed refrigerant stream, and recirculating the obtained condensed refrigerant stream to the high pressure evaporator (3) and a low pressure evaporator (2);
h. evaporating the condensed refrigerant stream in the low pressure evaporator (2) to obtain form refrigerant vapours and a condensed refrigerant stream, and recirculating the obtained condensed refrigerant stream to the high pressure evaporator (3) and the low pressure evaporator (2);
i. contacting the obtained refrigerant vapours with the third absorbent solution in the high pressure absorber (6) to obtain a fourth absorbent solution;
j. transferring the obtained fourth absorbent solution to first low temperature heat exchanger for heat exchange with the first absorbent solution, and further feeding to the low pressure absorber (7) for absorbing the refrigerant vapours obtained in step (h) to obtain a first absorbent solution;
k. transferring the obtained first absorbent solution to the first low temperature heat exchanger (16), the drain heat exchanger (17), the second low temperature heat exchanger (18) and the high temperature heat exchanger (19) and further feeding to the high temperature generator (21); and
l. repeating steps (a) to (k).
10. The method as claimed in claim 12, wherein said heat input is at least one selected from steam and superheated water; and wherein said heat input has a pressure in the range of 6 bar to 9 bar(g).
11. The method as claimed in claim 12, wherein the heat input at the outlet of HR (20) has a temperature in the range of 80oC to 99oC; said third absorbent solution has a temperature in the range of 88oC to 95oC.; said hot water in HWHE (23) has a temperature in the range of 60oC to 98oC; said water at the outlet of the EVAH (3) has a temperature in the range of 30oC to 40oC; and said cooling water pumped using pumping means (10) to the T-ABSL (24) has a temperature in the range of 25°C to 35°C.
Dated this 10th day of April, 2023

_______________________________
MOHAN RAJKUMAR DEWAN, IN/PA – 25
of R.K.DEWAN & CO.
Authorized Agent of Applicant

TO,
THE CONTROLLER OF PATENTS
THE PATENT OFFICE, AT MUMBAI