KR20000008670A - Ammonia GEX Absorption Cycle - Google Patents

Abstract

The present invention relates to an ammonia GAX absorption cycle that heats the generator and recovers maximum heat from the discharged combustion gas to improve the cycle coefficient of performance (COP).

One embodiment of the present invention, the generator 10 for generating a refrigerant vapor and a refrigerant aqueous solution (medicine solution) from the working solution (strong solution) by the heat generated by the burner, and the refrigerant vapor obtained from the generator 10 A condenser 20 for condensing the liquid refrigerant using cooling water, an evaporator 30 for evaporating the liquid refrigerant discharged from the condenser 20 again using cold water having an elevated temperature, and a refrigerant vapor, and the evaporator ( 30 is provided with an absorber 40 for producing a strong solution by the continuous absorption action to allow the drug vapor to absorb the refrigerant vapor generated in the 30, in the generator 10 GFD (11), SHD (12), The rectifier 13, the partial condenser 14, and the analyzer 15 is provided, The absorber 40 is provided with SCA 41, GAX 42, and HCA 43, The said GAX A portion of the steel solution flowing into the upper portion of the SHD 12 via the 42 is thermally bridged with the outlet combustion gas of the GFD 11. It is configured to include a secondary GFD (101) for supplying the upper portion of the SHD (12).

Description

Ammonia GEX Absorption Cycle

The present invention relates to an ammonia GAX absorption cycle, and more particularly, to an ammonia GAX absorption cycle that improves the Coefficient of Performance (COP) by heating the generator and recovering as much heat as possible from the discharged combustion gases. It is about.

In the conventional ammonia generator-absorber heat exchanger (GAX) absorption cycle, as shown in FIG. 1, refrigerant vapor is obtained by evaporating a refrigerant from a high concentration working solution (strong solution) by heat generated in a burner (not shown). At the same time, a generator 10 for generating a low concentration aqueous solution (medical solution) generated by evaporation of some refrigerant, and cooling water cooled after heat-exchanging the refrigerant vapor obtained by the generator 10 with external air in an outdoor unit are used. Condenser 20 to condense the liquid refrigerant, the evaporator 30 which evaporates the liquid refrigerant discharged from the condenser 20 again using cold water whose temperature rises from an indoor unit, and makes the refrigerant vapor, and the evaporator 30 Absorber 40 to form a strong concentration solution by the continuous absorption action to allow the drug vapor to absorb the refrigerant vapor generated in the) and the solution of the absorber 40 is a low pressure portion It consists of a solution pump (50) for sending to the generator 10, which is a high pressure portion, and a refrigerant heat exchanger (60) for exchanging the refrigerant vapor evaporated in the evaporator (30) with the liquid refrigerant condensed in the condenser (20). .

GFD (Gas-Fired Desorber, 11) for obtaining a refrigerant vapor by evaporating a refrigerant with a high temperature combustion gas in the generator 10 and at the same time generating a high-temperature medicinal solution with low concentration generated by evaporation of some refrigerant, and the GFD (11) condensing the medicinal solution produced in (11) and the SHD (Solution Heated Desorber, 12) sent to the absorber 40 while heat-exchanging with the strong solution supplied from the upper, and the refrigerant vapor of the high concentration by condensing water vapor evaporated with the refrigerant vapor Condensate part of the rectifier 13 and the refrigerant vapor passing through the rectifier 13 to the condenser 20 while cooling the refrigerant vapor with a strong solution supplied from the solution pump 50. The condenser 14, which is sent to the rectifier 13 and the temperature rises at the same time, is sent to the absorber 40, and the condensate is directly in contact with the refrigerant vapor in the rectifier 13. Raise the also which a riser Anna (Analyzer, 15) installed to increase the refrigerant vapor and the heat concentration is supplied to the upper portion rises at the bottom with a steel solution passed through the absorber (40).

SCA (Solution) for supplying a portion of the steel solution from the partial condenser 14 in the absorber 40 to the upper portion of the analyzer 15 after heat-exchanging to absorb a portion of the refrigerant vapor generated in the evaporator 30 Cooled Absorber (41) and the rest of the steel solution passed through the SCA (41) and the heat exchange to absorb some of the refrigerant vapor generated in the evaporator (30) and GAX (42) to send to the top of the SHD (12) and , Hydronic Cooled Absorber for cooling the heat generated by absorbing the refrigerant vapor generated by the evaporator 30 from the outdoor air with external air in the outdoor unit and then using the coolant to be cooled after passing through the SCA 41. 43 is installed.

Referring to the operation and operation of the conventional ammonia GAX absorption cycle configured as described above are as follows.

First, the principle of operation of the ammonia absorption cycle will be described based on the basic configuration to help technical understanding.

In the generator 10, an aqueous solution of a refrigerant, that is, an aqueous solution of ammonia, is present, which has a property of evaporating at a lower temperature than water.

Therefore, when the generator 10 is heated by a burner (not shown), water and ammonia are separated from each other. At this time, the ammonia that has not evaporated is lightly mixed with water, and this state is called a chemical solution state.

On the contrary, a state that is hardly separated is referred to as a strong solution state, and the separated pure ammonia undergoes heat exchange while passing through the condenser 20 and the evaporator 30.

At this time, since the generator 10 and the condenser 20 form a high pressure part, and the evaporator 30 and the absorber 40 form a low pressure part, the ammonia condensed in the condenser 20 immediately passes through the evaporator 30. While the heat exchange is carried out, the ammonia from the evaporator 30 is introduced into the absorber 40, the medicinal solution mixed with a little ammonia and the water produced in the generator 10 immediately enters the absorber 40, the evaporator ( It absorbs the ammonia from 30 and converts it back into a strong solution.

Next, the detailed operation of the conventional ammonia GAX absorption type cycle which applied the above operating principle is demonstrated.

First, when heat (about 1400-1600 ° C.) generated by a burner (not shown) is applied to the generator 10, the GFD 11 absorbs heat and is a strong solution (about 170 to 170) that is an operating solution in the GFD 11. 180 ° C.) is generated as a refrigerant vapor and a chemical solution (about 200 ° C.), and the refrigerant vapor flows into the rectifier 13 while rising.

At this time, the condenser 13 is condensed by the refrigerant vapor condensed by the strong solution supplied from the solution pump 50 in the partial condenser 14 so that the refrigerant vapor is rectified to the refrigerant vapor of a high concentration by the material transfer.

Then, the partial condenser 14 sends the refrigerant vapor passed through the rectifier 13 to the condenser 20, at the same time condenses a part to send the condensate back to the rectifier 13, and also from the lower part of the absorber 40 The temperature of the strong solution (approximately 50 ° C) suctioned through the 50) is increased to discharge the strong solution of about 70 ° C. The GAX (42) has been raised to a boiling point by the heat of absorption in the SCA (41). Is supplied.

The refrigerant vapor flowing into the condenser 20 is condensed into a liquid refrigerant through heat exchange with cooling water and then introduced into the evaporator 30, and the refrigerant vapor is again heated through heat exchange with cold water introduced into the evaporator 3 due to an increase in temperature in the indoor unit. Evaporated to cold water is sent to the indoor unit after the temperature drop by the latent heat of evaporation to perform the cooling.

Thereafter, the refrigerant vapor evaporated in the evaporator 30 passes through the refrigerant heat exchanger 60, and the temperature of the liquid refrigerant closes to the evaporation temperature in the evaporator 30 by heat exchange with the liquid refrigerant condensed in the condenser 20. As the temperature of the refrigerant vapor rises, the temperature of the refrigerant vapor rises near the temperature of the condensate exiting the condenser 20, and a small amount of refrigerant that does not evaporate in the evaporator 30 is also evaporated.

Then, the refrigerant vapor evaporated in the evaporator 30 is introduced into the absorber 40 after heat exchange in the refrigerant heat exchanger (60).

On the other hand, the refrigerant vapor generated in the GFD (11) and the remaining medicinal solution is supplied to the SHD (12) is heat exchanged with the steel solution supplied from the upper flows into the upper portion of the absorber 40 at a temperature lowered to about 150 ℃ .

The SCA 41 is supplied with a steel solution through the partial condenser 14 to cool a portion of the refrigerant vapor supplied through the refrigerant heat exchanger 60 to be absorbed by the medicinal solution, and then an analyser ( 15) and the remainder of the strong solution is supplied to the GAX 42 to cool the refrigerant vapor supplied through the refrigerant heat exchanger 60 to absorb some of the medicinal solution, and then the temperature is raised to SHD (12). It is supplied to the top of).

Here, the steel solution introduced into the SCA 41 is heated by the absorption heat generated when the refrigerant vapor is absorbed into the chemical solution in the absorber 40 so that the temperature rises to the boiling point (about 100 ° C.), and the GAX 42 The strong solution introduced into the is heated by the absorption heat generated when the refrigerant vapor is absorbed into the medicinal solution to start boiling, and is supplied to the upper portion of the SHD 12 in a gas-liquid abnormal flow state (about 140 ° C.).

Then, the steel solution introduced into the upper portion of the SHD 12, which is the middle temperature portion of the generator 10, through the GAX 42 after heat exchange with the chemical solution, exchanges heat with the chemical solution flowing in the SHD 12 in the generator 10. And then descend.

In addition, the steel solution introduced into the SCA 41 exchanges heat with the GAX 42 to desorb the heat of absorption when the chemical solution whose temperature is lowered absorbs the refrigerant vapor, thereby increasing the temperature and causing the analyzer 15 to rise in the generator 10. While entering the upper portion of the generator 10, while contacting with the refrigerant vapor generated and rises, while absorbing some of the water vapor contained in the refrigerant vapor to rectify the temperature rises to a lower portion in the generator (10).

At this time, in the ammonia GAX absorption cycle, the cold water whose temperature has been dropped from the evaporator 30 is cooled to the indoor unit to cool the air, and the cooling water that cools the condenser 20 and the HCA 43 increases in temperature, thereby cooling it again to the outdoor unit. do.

On the contrary, in the case of heating, cold water whose temperature is increased while passing through the condenser 20 and the absorber 40 is sent to the indoor unit to perform heating, and the cooling water that has passed through the evaporator 30 is sent to the outdoor unit.

The above operation is continuously circulated while the system is in equilibrium.

In the ammonia GAX absorption cycle as described above, GFD is a kind of high temperature heat exchanger that exchanges heat with the combustion gas, which takes heat from the combustion gas to generate most of the refrigerant vapor, while supplying a weak concentration of the hot chemical solution to the absorber. It is the most basic element to absorb refrigerant vapor.

The thermal efficiency of the GFD is determined by how much heat is taken from the combustion gas. That is, Equations 1 and 2 below may be set as a ratio of the heat of absorption of the GFD to the gas consumption Q _gas Q _GFD .

η = Q _GFD / Q _gas

Q _GFD = G _exh × (h _{exh, i} -h _{exh, o} ) = Combustion gas flow rate × (entrance enthalpy-exit enthalpy)

However, the generator thermal efficiency of the absorption system is very low compared to the thermal efficiency of the hot water boiler. The reason is that in the case of boilers, the temperature of the fluid (hot water) that exchanges heat with the combustion gas is about 50 to 70 ° C, whereas in the case of absorption heat pumps, it is about 100 ° C higher than that of the boiler.

Therefore, there is a problem that the absorption system does not utilize the heat of combustion efficiently.

Referring to the schematic diagram of the GFD shown in FIG. 2, the heat efficiency of the heat exchanger based on the enthalpy of the combustion gas may be obtained by Equation 3 below.

In the figure, T _{exh, i} is the inlet flue gas temperature, T _{exh, o} is the outlet flue gas temperature, T _{s, i} is the steel solution temperature, T _{v, o} is the refrigerant vapor temperature, and T _{s, o} Is the chemical solution temperature.

Where G _exh is the combustion gas flow rate, G _fuel is the fuel consumption, and λ is the calorific value per unit weight of the fuel.

In addition, when the temperature of the exit flue gas is T´ _{exh, o} and T _{exh, o} , the amount of heat received by the GFD is Q´ _GFD and Q _GFD , respectively. Equation 4

In addition, if the sum of the efficiency change amount Δη / ΔT _exh per 1 ° C outlet gas temperature is expressed by the excess air ratio α and the like during fuel combustion can be expressed by the following equation (5).

Where m _O2 is the number of moles of oxygen required for combustion per mol of fuel, M _fuel is the molar equivalent of fuel, M _O2 is the molar equivalent of oxygen, M _N2 is the molar equivalent of nitrogen, and C _p is Specific heat of combustion gas.

On the other hand, the generator inlet temperature of the GAX absorption system is about 170 ° C. although there may be some differences depending on the type of the high temperature heat exchanger. Regardless of the size of the heat exchanger, the outlet temperature of the flue gas never exceeds the solution inlet temperature, and the heat exchanger is infinitely large so that the maximum thermal efficiency η _max is obtained when the outlet flue gas temperature is equal to the solution inlet temperature.

That is, T _{exh, o} ≥ T _{s, i} is always obtained _, and the maximum thermal efficiency that can be obtained is T _{exh, o} = T _{s, i} in FIG. 2, where thermal efficiency η _max is expressed by Equation 6 below from Equation 3 below. Can be represented.

The difference between the maximum thermal efficiency and the actual thermal efficiency is due to the enthalpy difference, which is the difference between the lowest outlet flue gas temperature (T _{s, i} ) and the actual flue gas temperature that can ultimately be achieved. it means. This can be expressed simply from Equation 4 as shown in Equation 7 below.

The above facts assume, for example, the complete combustion of methane (CH ₄ ) in the combustion of natural gas and the thermal efficiency according to the change in the outlet combustion gas temperature of 1 ° C when α = 0.7 (generally the excess air ratio is 07 to 0.8). The change amount can be calculated from Equation 5 as shown in Equation 8 below.

That is, there is a change in thermal efficiency of 0.065% per 1 ° C. of the outlet flue gas temperature change. Comparing this to the case of the hot water boiler and the absorption type heat pump generator, it is possible to guess how much the thermal efficiency of the generator is lowered.

For example, when the inlet temperature of the hot water boiler is 50 ° C. and the generator inlet temperature is 100 ° C. higher than 150 ° C., the difference (Δη _max ) between the respective maximum thermal efficiencies is represented by Equation 9 from Equation 3 below. .

That is, in the case of the generator, even if the thermal efficiency is excellent, it can be seen that the theoretical thermal efficiency is about 7% lower than that of the hot water boiler. This fundamental reduction in thermal efficiency is due to the solution temperature at the generator inlet.

Therefore, the present invention has been proposed to solve the above-described problems of the thermal efficiency, the first: firstly heat-exchanging the combustion gas heat-exchanged with the working solution and the second working solution, and second: second heat exchange The working solution temperature is low enough to effectively recover energy from the combustion gas, thereby reducing the temperature of the final discharged gas as much as possible to improve the cycle coefficient of performance (COP). will be.

Technical means of the present invention for achieving this object, a generator for generating a refrigerant vapor and a medicinal solution from a strong solution by the heat generated in the burner, a condenser for condensing the refrigerant vapor into a liquid refrigerant using a cooling water, and An evaporator which evaporates the liquid refrigerant again by using cold water whose temperature has risen to become a refrigerant vapor, an absorber which forms a strong solution by a continuous absorption action by which the chemical solution absorbs the refrigerant vapor generated in the evaporator, and A solution pump for sending the solution to the generator and a refrigerant heat exchanger for exchanging the refrigerant vapor evaporated in the evaporator with the liquid refrigerant condensed in the condenser, the generator comprises a GFD, SHD, rectifier, partial condenser, and an analyzer In the ammonia GAX absorption type cycle equipped with SCA, GAX, and HCA in an absorber, the steel which flows in the predetermined place in a cycle A part of the solution is characterized in that it comprises a secondary GFD which is supplied to the generator by heat exchange with the outlet combustion gas of the GFD.

1 is a conventional ammonia (GAX) absorption cycle diagram.

FIG. 2 is a schematic diagram of the GFD shown in FIG. 1. FIG.

Figure 3 is an ammonia GAX absorption cycle diagram according to a first embodiment of the present invention.

Figure 4 is an ammonia GAX absorption cycle diagram according to a second embodiment of the present invention.

5 is an ammonia GAX absorption cycle diagram according to a third embodiment of the present invention.

6 is an ammonia GAX absorption cycle diagram according to a fourth embodiment of the present invention.

*** Explanation of symbols for the main parts of the drawing ***

10: generator 11: GFD

12: SHD 14: partial condenser

15: analyzer 40: absorber

41: SCA 42: GAX

50: solution pump 101: auxiliary GFD

Hereinafter, the present invention will be described with reference to the accompanying drawings.

<First Embodiment>

Figure 3 shows ammonia GAX absorption cycle diagram according to a first embodiment of the present invention, the same configuration as the conventional cycle shown in Figure 1 denote the same reference numerals.

As shown, generator 10, condenser 20, evaporator 30, absorber 40, solution pump 50, refrigerant heat exchanger 60, GFD 11, SHD 12, rectifier ( 13), in an absorption cycle with a partial condenser 14, an analyzer 15, an SCA 41, a GAX 42, an HCA 43, via the GAX 42 of the SHD 12 It comprises a secondary GFD (101) for supplying to the upper portion of the SHD (12) by heat-exchanging a portion of the steel solution flowing into the upper portion with the outlet combustion gas of the GFD (11).

The operation and effect of the ammonia GAX absorption cycle according to the first embodiment of the present invention configured as described above will be described with reference to FIG. 3, and the same functions as those of the conventional ammonia GAX absorption cycle shown in FIG. It is omitted to avoid.

First, when heat generated from a burner (not shown) is applied to the generator 10, the GFD 11 absorbs heat, and a strong solution, which is an operating solution in the generator 10, is generated as a refrigerant vapor and a chemical solution. The refrigerant vapor is raised in the generator 10.

In addition, the medicinal solution that sinks to the lower portion due to the higher specific gravity than the strong solution in the generator 10 is heat-exchanged through the SHD 12, and then the absorber (by the pressure difference between the high pressure generator 10 and the low pressure absorber 40). 40) flows to the top.

On the other hand, the strong solution flowing into the GAX 42 heats when the medicinal solution absorbs the refrigerant vapor and starts boiling, and is supplied to the upper portion of the SHD 12 in a gas-liquid transient state, where a part of the strong solution is branched. Supplied to the secondary GFD 101.

Then, the auxiliary GFD 101 exchanges the steel solution with the outlet combustion gas of the GFD 11 and supplies it back to the top of the SHD 12.

Subsequently, the strong solution introduced into the upper portion of the SHD 12, which is the mid temperature portion of the generator 10, through the GAX 42 and the auxiliary GFD 101 is uniformly dispersed in the generator 10 to flow in the SHD 12. After exchanging heat with chemical solution, it descends.

For example, the ε (heat exchanger effectiveness) of the GFD (11) and the auxiliary GFD (101) is ε _main = 0.95 and ε _sub = 0.5, and the inlet temperature T ₁ = 170 ° C. of the GFD 11, respectively, and the auxiliary GFD When the inlet temperature T _{2 of} 140 is 140 ° C., the excess combustion air ratio α is 0.7 and the flame temperature T ₃ = 1400 ° C.,

Combustion gas exit temperature of GFD (11) T exit of the temperature of the combustion gas ₄ and the auxiliary GFD (101) T ₅ is shown in Equation 10 and 11 below, respectively.

That is, the temperature of the finally discharged combustion gas was lowered from 232 ° C to 186 ° C by heat-exchanging the low temperature solution (140 ° C) leaving the GAX 42 in the auxiliary GFD 101 with the combustion gas.

At this time, the improvement effect of the generator thermal efficiency compared to the conventional cycle shown in Figure 1 is calculated as shown in Equation 12 below.

Δη _UP = 0.065 × (232-186) ≒ 3.0%

This heat efficiency rise indicates the amount of heat recovery in the auxiliary GFD 101, and the amount of refrigerant vapor in the system increases by that amount, thereby increasing the COP.

Second Embodiment

Figure 4 shows ammonia GAX absorption cycle diagram according to a second embodiment of the present invention, the same configuration as the conventional cycle shown in Figure 1 denote the same reference numerals.

As shown, generator 10, condenser 20, evaporator 30, absorber 40, solution pump 50, refrigerant heat exchanger 60, GFD 11, SHD 12, rectifier ( 13) in an absorption cycle with a partial condenser 14, an analyzer 15, an SCA 41, a GAX 42, and an HCA 43, via the SCA 41 and the analyzer 15 A part of the steel solution flowing into the upper portion of the secondary GFD 101 for selectively supplying any one of the upper portion of the SHD 12 and the upper portion of the analyzer 15 by heat-exchanging with the outlet combustion gas of the GFD 11. It is configured to include.

The operation and effect of the ammonia GAX absorption cycle according to the second embodiment of the present invention configured as described above will be described with reference to FIG. 4, and the same functions as those of the conventional ammonia GAX absorption cycle shown in FIG. It is omitted to avoid.

First, when heat generated from a burner (not shown) is applied to the generator 10, the GFD 11 absorbs heat, and a strong solution, which is an operating solution in the generator 10, is generated as a refrigerant vapor and a chemical solution. The refrigerant vapor is raised in the generator 10.

In addition, the medicinal solution that sinks to the lower portion due to the higher specific gravity than the strong solution in the generator 10 is heat-exchanged through the SHD 12, and then the absorber (by the pressure difference between the high pressure generator 10 and the low pressure absorber 40). 40) flows to the top.

On the other hand, the SCA 41 is supplied with a steel solution passed through the partial condenser 14 to heat the refrigerant vapor generated in the evaporator 30 to absorb some of the medicinal solution and then supply a portion to the upper portion of the analyzer 15 , The remainder of the steel solution is heat-exchanged to absorb a portion of the refrigerant vapor generated in the evaporator 30 via the GAX 42 and then supplied to the top of the SHD (12).

Here, the steel solution introduced into the SCA 41 is heated by the absorption heat generated when the refrigerant vapor is absorbed into the medicinal solution in the SCA 41 so that the temperature rises to a boiling point (about 100 ° C.). A portion is branched and fed to the secondary GFD 101.

The auxiliary GFD 101 then heats this steel solution with the outlet combustion gas of the GFD 11 and supplies it back to the top of the analyzer 15 or the top of the SHD 12.

If the auxiliary GFD 101 supplies the strong solution to the upper portion of the SHD 12, the secondary GFD 101 flows into the upper portion of the SHD 12, which is the mid temperature portion of the generator 10, through the GAX 42 and the auxiliary GFD 101. The strong solution is uniformly dispersed in the generator 10 and heat-exchanged with the chemical solution flowing in the SHD 12, and then descends.

When the auxiliary GFD 101 supplies the strong solution to the upper portion of the analyzer 15, the auxiliary GFD 101 is uniformly dispersed in the generator 10, and the dispersed steel solution rises through the analyzer 15. After absorbing some of the water vapor contained therein to rectify, the temperature is lowered and lowered to the bottom of the generator (10).

As described above, the second embodiment of the present invention provides the auxiliary GFD 101 as a temperature (about 100 ° C) at which the solution temperature at the outlet of the SCA 41 is lower than the solution temperature at the outlet of the GAX 42 as compared with the first embodiment described above. Can lower the temperature of the combustion gases passing through

For example, the ε of the GFD 11 and the auxiliary GFD 101 are ε _main = 0.95 and ε _sub = 0.5, the inlet temperature T ₁ = 170 ° C. of the GFD 11, respectively, and the inlet of the auxiliary GFD 101. when the temperature T ₂ and = 100 ℃, excess combustion air ratio (α) = 0.7, and the flame temperature T ₃ = 1400 ℃,

The outlet combustion gas temperature T ₄ of the GFD 11 is represented by Equation 10, and the outlet combustion gas temperature T ₅ of the auxiliary GFD 101 is represented by Equation 13 below.

That is, the temperature of the finally discharged combustion gas was lowered from 232 ° C. to 166 ° C. by heat-exchanging the low temperature solution (100 ° C.) leaving the GAX 42 in the auxiliary GFD 101 with the combustion gas.

At this time, the improvement effect of the generator thermal efficiency compared to the conventional cycle shown in Figure 1 is calculated as shown in Equation 14 below.

Δη _UP = 0.065 × (232-166) ≒ 4.3%

The heat efficiency rise indicates the amount of heat recovery in the auxiliary GFD 101, and the flow rate branched from the outlet of the SCA 41 to the auxiliary GFD 101 is determined to be optimal through the basic experiment.

Third Embodiment

FIG. 5 shows a cycle diagram of the ammonia GAX absorption type according to the third embodiment of the present invention, in which the same components as in the conventional cycle shown in FIG. 1 denote the same reference numerals.

As shown, generator 10, condenser 20, evaporator 30, absorber 40, solution pump 50, refrigerant heat exchanger 60, GFD 11, SHD 12, rectifier ( 13) in an absorption cycle with a partial condenser 14, an analyzer 15, an SCA 41, a GAX 42, an HCA 43, via the partial condenser 14 the SCA 41 A secondary GFD (101) for selectively supplying any one of the upper portion of the SHD (12) and the upper portion of the analyzer 15 by heat-exchanging a portion of the steel solution flowing into the outlet combustion gas of the GFD (11) It is composed by.

The operation and effect of the ammonia gas-absorption cycle according to the third embodiment of the present invention configured as described above will be described with reference to FIG. 5, and the same functions as those of the conventional ammonia gas-absorption cycle shown in FIG. It is omitted to avoid.

First, when heat generated from a burner (not shown) is applied to the generator 10, the GFD 11 absorbs heat, and a strong solution, which is an operating solution in the generator 10, is generated as a refrigerant vapor and a chemical solution. The refrigerant vapor is raised in the generator 10.

In addition, the medicinal solution that sinks to the lower portion due to the higher specific gravity than the strong solution in the generator 10 is heat-exchanged through the SHD 12, and then the absorber (by the pressure difference between the high pressure generator 10 and the low pressure absorber 40). 40 is introduced into the upper portion, and is cooled while passing through the GAX 42, the SCA 41, and the HCA 43 in order to absorb the refrigerant vapor, thereby producing a strong solution (about 50 ° C).

Meanwhile, the steel solution sucked from the lower part of the absorber 40 by the solution pump 50 becomes a strong solution of about 70 ° C. while condensing a part of the refrigerant in the partial condenser 14, and is supplied into the absorber 40. A portion is branched and fed to the secondary GFD 101.

The auxiliary GFD 101 then heats this steel solution with the outlet combustion gas of the GFD 11 and supplies it back to the top of the analyzer 15 or the top of the SHD 12.

Thereafter, the heat exchange process in the generator 10 is the same as in the above-described second embodiment, and a description thereof will be omitted.

As such, the third embodiment of the present invention is the temperature of the combustion gas passing through the auxiliary GFD 101 as the solution temperature at the outlet of the partial condenser 14 is much lower than the solution temperature at the inlet of the GFD 11 (about 70 ° C.). Can be lowered.

For example, the ε of the GFD 11 and the auxiliary GFD 101 are ε _main = 0.95 and ε _sub = 0.5, the inlet temperature T ₁ = 170 ° C. of the GFD 11, respectively, and the inlet of the auxiliary GFD 101. When the temperature T ₂ = 70 ° C., the excess combustion air ratio α = 0.7 and the flame temperature T ₃ = 1400 ° C.,

The outlet combustion gas temperature T ₄ of the GFD 11 is represented as in Equation 10, and the outlet combustion gas temperature T ₅ of the auxiliary GFD 101 is represented as in Equation 15 below.

That is, the temperature of the finally discharged combustion gas was lowered from 232 ° C. to 151 ° C. by heat-exchanging the low temperature solution (70 ° C.) leaving the partial condenser 14 in the auxiliary GFD 101 with the combustion gas.

At this time, the improvement effect of the generator thermal efficiency compared to the conventional cycle shown in Figure 1 is calculated as shown in Equation 16 below.

Δη _UP = 0.065 × (232-151) ≒ 5.3%

This thermal efficiency rise indicates the amount of heat recovery in the auxiliary GFD 101, and the flow rate branched from the outlet of the partial condenser 14 to the auxiliary GFD 101 is determined to be an optimal value through basic experiments.

Fourth Example

Figure 6 shows ammonia GAX absorption cycle diagram according to a fourth embodiment of the present invention, the same configuration as the conventional cycle shown in Figure 1 denote the same reference numerals.

As shown, generator 10, condenser 20, evaporator 30, absorber 40, solution pump 50, refrigerant heat exchanger 60, GFD 11, SHD 12, rectifier ( 13), in an absorption cycle with a partial condenser 14, an analyzer 15, an SCA 41, a GAX 42, and an HCA 43, is ejected from the solution pump 50 and the partial condenser ( 14) the auxiliary GFD 101 for selectively supplying one of the upper portion of the SHD 12 and the upper portion of the analyzer 15 by heat-exchanging a portion of the steel solution flowing into the outlet combustion gas of the GFD 11. It is configured to include.

The operation and effect of the ammonia gas-absorption cycle according to the fourth embodiment of the present invention configured as described above will be described with reference to FIG. 6, and the same functions as those of the conventional ammonia gas-absorption cycle shown in FIG. It is omitted to avoid.

First, when heat generated from a burner (not shown) is applied to the generator 10, the GFD 11 absorbs heat, and a strong solution, which is an operating solution in the generator 10, is generated as a refrigerant vapor and a chemical solution. The refrigerant vapor is raised in the generator 10.

In addition, the medicinal solution that sinks to the lower portion due to the higher specific gravity than the strong solution in the generator 10 is heat-exchanged through the SHD 12, and then the absorber (by the pressure difference between the high pressure generator 10 and the low pressure absorber 40). 40 is introduced into the upper portion and evenly distributed, and heat-exchanged while passing through the GAX 42, SCA 41 and HCA 43 in order to produce a strong solution (about 50 ℃).

Meanwhile, the solution pump 50 sucks the strong solution from the lower part of the absorber 40 and ejects it to the partial condenser 14, where a part of the strong solution is branched and supplied to the auxiliary GFD 101.

The auxiliary GFD 101 then heats this steel solution with the outlet combustion gas of the GFD 11 and supplies it back to the top of the analyzer 15 or the top of the SHD 12.

Since the heat exchange process in the generator 10 is the same as the above-described second and third embodiments, description thereof will be omitted.

As such, the fourth embodiment of the present invention is the temperature of the combustion gas passing through the auxiliary GFD 101 as the solution temperature at the inlet of the partial condenser 14 is much lower than the solution temperature at the inlet of the GFD 11 (about 50 ° C.). Can be lowered.

For example, the ε of the GFD 11 and the auxiliary GFD 101 are ε _main = 0.95 and ε _sub = 0.5, the inlet temperature T ₁ = 170 ° C. of the GFD 11, respectively, and the inlet of the auxiliary GFD 101. When the temperature T ₂ = 50 ° C., the excess combustion air ratio α = 0.7 and the flame temperature T ₃ = 1400 ° C.,

The outlet combustion gas temperature T ₄ of the GFD 11 is represented by Equation 10, and the outlet combustion gas temperature T ₅ of the auxiliary GFD 101 is represented by Equation 17 below.

That is, the temperature of the finally discharged combustion gas was lowered from 232 ° C to 141 ° C by heat-exchanging the low temperature solution (50 ° C) ejected from the solution pump 50 with the combustion gas in the auxiliary GFD 101.

At this time, the improvement effect of the generator thermal efficiency compared to the conventional cycle shown in Figure 1 is calculated as shown in Equation 18 below.

Δη _UP = 0.065 × (232-141) ≒ 5.9%

The heat efficiency rise indicates the amount of heat recovery in the auxiliary GFD 101, and the flow rate branched from the outlet of the solution pump 50 to the auxiliary GFD 101 is determined to be an optimal value through a basic experiment.

As described above, in the present invention, the combustion gas primarily heat-exchanged with the working solution is secondly heat-exchanged with the working solution, but the temperature of the working solution that is secondarily heat-exchanged is low enough to effectively recover energy from the combustion gas. By having a, it is possible to lower the temperature of the final discharged gas as much as possible to improve the performance coefficient (COP) of the cycle.

Claims (5)

A generator for generating a refrigerant vapor and an aqueous refrigerant solution (medical solution) from the working solution (strong solution) by the heat generated by the burner, a condenser for condensing the refrigerant vapor obtained from the generator with a liquid refrigerant using cooling water, and in the condenser An evaporator for evaporating the discharged liquid refrigerant again by using cold water of elevated temperature to form a refrigerant vapor, an absorber for forming a strong solution by a continuous absorption action of allowing the chemical solution to absorb the refrigerant vapor generated in the evaporator, A solution pump for sending the solution of the absorber to the generator, and a refrigerant heat exchanger for exchanging the refrigerant vapor evaporated in the evaporator with the liquid refrigerant condensed in the condenser. SHD), a rectifier, a partial condenser, and an analyzer, and in the absorber, SCA and Jie In an ammonia jieyi X (GAX) cycle having an absorption X (GAX) and H. Associates (HCA), An ammonia GS absorption cycle comprising an auxiliary GFD (GFD) for exchanging a part of the steel solution introduced into a predetermined part of the cycle with the outlet combustion gas of the GFD to be supplied into the generator. The method of claim 1, The auxiliary GFD heat exchanges a portion of the steel solution flowing into the upper portion of the SHD via the GAX and supplies the upper portion of the SHD by exchanging heat with the outlet combustion gas of the GFD. The method of claim 1, The auxiliary GFD heat-exchanges a part of the steel solution flowing into the upper portion of the analyser through the SCA with the outlet combustion gas of the GFD, and selectively supplies any one of the upper portion of the SHD and the upper portion of the analyzer. Ammonia GS Absorption Cycle. The method of claim 1, The auxiliary GFD heat-exchanges a part of the steel solution flowing into the SCA through the partial condenser with the outlet combustion gas of the GFD to selectively supply any one of the upper part of the SHD and the upper part of the analyzer. GE X Absorption Cycle. The method of claim 1, The auxiliary GFD heats a part of the steel solution ejected from the solution pump and flows into the partial condenser with the outlet combustion gas of the GFD, thereby selectively supplying any one of the upper part of the SHD and the upper part of the analyzer. Ammonia GS Absorption Cycle.