JP2935653B2 - Absorption chiller / heater and operation control method thereof - Google Patents

Description

DETAILED DESCRIPTION OF THE INVENTION

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a high-quality fuel system and an exhaust heat utilization system, and an external exhaust heat (for example, a cogeneration system) via a heat exchanger interposed in a pipe of the exhaust heat utilization system. The present invention relates to an absorption chiller / heater into which a fluid at 30 ° C. to 120 ° C. generated from the above, such as hot water or steam, is charged.

[0002]

2. Description of the Related Art With respect to such technology, the present applicant has filed Japanese Patent Application No.
No. 73428 will be described.

In FIG. 29, an absorption chiller / heater 1 comprises an evaporator 9, an absorber 10, a high temperature regenerator 11, a low temperature regenerator 12,
A condenser 13, a high-temperature solution heat exchanger 14, a low-temperature solution heat exchanger 15, a refrigerant pump P9, a solution pump P10, and various lines connecting these members are provided. A chilled water line 6 for supplying chilled water to a cooling load (not shown)
And a fuel line 7 for supplying high-quality fuel to a heating source (for example, a gas burner) for the high-temperature regenerator 11. Further, a cooling water line CL for supplying cold water to the absorber 10 and the condenser 13 is provided, and circulates cooling water cooled by a cooling tower (not shown). The diluted solution line L between the high-temperature solution heat exchanger 14 and the low-temperature solution heat exchanger 15
1 is provided with a heat source heat exchanger 5. In the heat source heat exchanger 5, a hot waste water flowing through a waste heat line L 2 of a cogeneration system (not shown) and an absorber 1 are provided.
From 0, the diluted solution flowing through the diluted solution line L1 via the pump P10 exchanges heat. That is, the heat source heat exchanger 5 transfers a part of the amount of heat of the waste water at 85 ° C. to 120 ° C. to the dilute solution flowing through the dilute solution line L1, thereby increasing the cost of the high-quality fuel. It is designed to reduce the amount of consumption.

[0004]

The technique proposed above is very effective. However, in recent years, demands for energy saving are severe, and a reduction rate of high-quality fuel consumption is demanded to be about 20% to 40%. On the other hand, in the above-described conventional technology, the reduction rate of high-quality fuel at the time of rating is about 12%, and it is difficult to cope with the strict requirements described above.

The present invention has been proposed in view of the above-mentioned problems of the prior art, and provides an absorption chiller / heater capable of further increasing the waste heat utilization rate and reducing the consumption of high quality fuel. The purpose is.

[0006]

[Knowledge] As a result of various studies, the present inventor has found that, in the above prior art, a heat source heat exchanger 5 interposed in the dilute solution line L1 was used.
The heat exchange performed in is a sensible heat and sensible heat exchange performed between the liquid phase and the liquid phase, but when the diluted solution is decompressed and sent to the heat exchanger,
We paid attention to the fact that a part of the diluted solution undergoes a phase change, that is, vaporization, deprives the heat exchanger of heat of vaporization, that is, latent heat, and exchanges sensible heat and latent heat. When such sensible heat / latent heat exchange is performed, the dilute solution deprives the calorific waste water of a larger amount of heat than the conventional sensible heat / sensible heat exchange, thereby improving the heat exchange rate. I found that. The present invention has been created based on such knowledge.

[0007]

SUMMARY OF THE INVENTION An absorption chiller / heater of the present invention comprises a dilute solution line from an absorber to a low temperature regenerator via a low temperature solution heat exchanger, a low temperature regenerator to a solution pump and a high temperature solution heat exchange. An intermediate-concentration solution line directed to a high-temperature regenerator via a heat exchanger, and a pressure adjusting means and an intermediate regenerator interposed between the low-temperature solution heat exchanger and the low-temperature regenerator in the dilute solution line. The hot water drain port performs sensible heat / latent heat exchange between the fluid supplied from the external heat source and the fluid in the dilute solution line, and measures the inflow temperature of the fluid supplied from the external heat source. The operation mode of the absorption chiller / heater is increased based on the temperature sensor, the chilled water outlet temperature sensor that measures the temperature of the chilled water flowing out from the evaporator to the cooling load side, and the outputs of the hot water drain inlet temperature sensor and the chilled water outlet temperature sensor. High-quality fuel-only operation mode Heat-up and Koshitsu fuel firing operation mode, control means for determining the one of the exhaust heat alone turned operation mode, and a capital.

Here, for example, a pressure reducing valve is used as the pressure adjusting means.

In implementing the absorption chiller / heater of the present invention, heat for a heat source for performing sensible heat / sensible heat exchange between a fluid supplied from an external heat source and an intermediate concentration solution flowing through an intermediate concentration solution line. Preferably, an exchanger is provided. At that time,
It is also possible to provide a composite intermediate regenerator in which the intermediate regenerator and a part of the heat source heat exchanger are integrated.

[0010] In addition to the pressure adjusting means, an auxiliary pressure adjusting means may be provided. In this case, the number of auxiliary pressure adjusting means may be one or two or more.
The number or location of the auxiliary pressure adjusting means is set so that the pressure balance of the entire system can be adjusted well.

Here, in the circulation system of the absorption chiller / heater,
If the pressure is set, the flow rate is uniquely determined, and if the flow rate is set, the pressure is uniquely determined. That is, the pressure and the flow rate are determined in a one-to-one relationship. Therefore, it is preferable to provide the pressure adjusting means and the auxiliary pressure adjusting means as flow rate adjusting means such as a variable orifice.

Further, in addition to the cold water outlet sensor and the cold water outlet temperature sensor, a cooling water inlet temperature sensor for measuring a cooling water inflow temperature may be provided.

An intermediate pressure measuring means for measuring the pressure of the low-temperature regenerator or a pressure of the condenser; a low-temperature regenerator temperature measuring means for measuring the temperature of the low-temperature regenerator; A means selected from dilute solution pressure measuring means for measuring the pressure or dilute solution temperature measuring means for measuring the temperature may be provided.

The operation method of the absorption chiller / heater according to the present invention includes a dilute solution line from an absorber to a low-temperature regenerator via a low-temperature solution heat exchanger, and a low-temperature regenerator via a solution pump and a high-temperature solution heat exchanger. An operation control method of an absorption chiller / heater of the type having an intermediate concentration solution line directed toward a high temperature regenerator, comprising: a pressure adjusting means and an intermediate regenerator between the low temperature regenerator and the low temperature solution heat exchanger of the dilute solution line. The intermediate regenerator performs sensible heat / latent heat exchange between the fluid supplied from the external heat source and the fluid in the dilute solution line, and receives the fluid supplied from the external heat source. Based on the measured temperature of the warm water drain and the temperature of the warm water drain, and the temperature of the cold water outlet measuring the temperature of the cold water flowing out from the evaporator to the cooling load side. Operation of chiller / heater O de Koshitsu fuel alone firing operation mode, exhaust heat-up and Koshitsu fuel firing operation mode, the operation mode determining step of determining the one of the exhaust heat alone turned operation mode, and a capital.

A cooling water inlet temperature measuring step for measuring the inflow temperature of the cooling water, an intermediate pressure measuring step for measuring the pressure of the low temperature regenerator or the pressure of the condenser,
A low-temperature regenerator temperature measurement process for measuring the temperature of the low-temperature regenerator,
A step selected from a dilute solution pressure measuring step for measuring the pressure of the dilute solution on the low temperature regenerator side of the pressure adjusting means or a dilute solution temperature measuring step for detecting the temperature may be provided.

According to the present invention having the configuration as described above, by performing sensible heat / latent heat exchange with a large amount of heat transfer, compared with the conventional sensible heat / sensible heat exchange only technology, More heat can be supplied from the exhaust heat into the absorption chiller / heater. As a result, it is possible to increase the waste heat utilization rate and reduce the consumption of high quality fuel, and approach the target value of 20 to 40%.

Then, the inflow temperature of the fluid supplied from the external heat source, the temperature of the chilled water supplied to the cooling load side, the inflow temperature of the cooling water, the pressure of the low-temperature regenerator or the pressure of the condenser,
Various operating conditions, such as the temperature of the low-temperature regenerator, the pressure or temperature of the dilute solution on the low-temperature regenerator side of the pressure adjusting means, etc., are selectively controlled elements, and in a manner described later, the exhaust heat-fired single operation, One of the operation modes of the high quality fuel burning alone operation, the exhaust heat and the high quality fuel burning operation can be selected. Further, it is possible to adjust the flow rate to the optimum in various operation modes.

As a result, in the operation of the absorption chiller / heater,
It is possible to control the pressure or flow balance with very high accuracy.

[0019]

Embodiments of the present invention will be described below with reference to the drawings. In these drawings, FIG.
The same reference numerals are given to the portions corresponding to and the duplicate description will be omitted. Here, the present invention is directed to a so-called “reverse type” absorption chiller / heater in which a dilute solution line is directed to a low-temperature regenerator, and a low-concentration solution line is directed to a high-temperature regenerator.

The absorption chiller / heater shown in FIG. 1 includes a dilute solution line L1 extending from the absorber 10 through the low-temperature solution heat exchanger 15 to the low-temperature regenerator 12, and a low-temperature regenerator 12 and a solution pump P1.
2 and an intermediate concentration solution line L3 toward the high temperature regenerator 11 via the high temperature solution heat exchanger 14, and from the high temperature regenerator 11 to the absorber 10 via the high temperature solution heat exchanger 14 and the low temperature solution heat exchanger 15. A high-concentration solution line L4 is provided, and is configured as a so-called “reverse type”.

The low-temperature solution heat exchanger 15 of the dilute solution line L1
A pressure reducing valve 17 serving as a pressure adjusting means and an intermediate regenerator 18 are interposed between the low temperature regenerator 12 and the low temperature regenerator 12. A waste heat line L2 is connected to the intermediate regenerator 18, and heat exchange between hot waste water in the waste heat line L2 and the dilute solution flowing through the dilute solution line L1 (sensible heat / latent heat exchange as described later). It is supposed to do. Further, the pressure reducing valve 17 has an effect of lowering the pressure in the diluted solution line L1 and decreasing the regeneration temperature of the diluted solution. At the same time, the flow rate and pressure in the line system circulating in the absorption chiller / heater need to be finely adjusted and balanced, so that the pressure reducing valve 17 serves as a flow rate / pressure adjusting means.

Further, a control unit 30 as a control means is provided, and the control unit 30 includes a fuel control valve 3
1. A three-way valve 32 for hot drainage, a hot drain outlet temperature sensor 33 for measuring the hot drain inlet temperature Th of the exhaust heat line L2, and a cold water outlet temperature sensor for measuring the cold outlet temperature T1 flowing from the evaporator 9 to the cooling load side. 34, a cooling water inlet temperature sensor 35 for measuring the cooling water inlet temperature Tm of the cooling line CL, an intermediate pressure sensor 36 for measuring the pressure of the low temperature regenerator 12 or a low temperature regenerator temperature sensor 37 for measuring the temperature, and a branch line L3. The dilute solution pressure sensor 3 which is a dilute solution pressure measuring means for measuring the pressure of the dilute solution on the low temperature regenerator 12 side of the pressure reducing valve 17
8 or a dilute solution temperature sensor 39 which is a dilute solution temperature measuring means for measuring the temperature of the dilute solution.

In the illustrated embodiment, the high-temperature regenerator 11 is described as performing high-quality fuel burning using a gas burner, but high-quality fuel burning is not limited to the use of a gas burner. Although not shown,
For example, high-temperature steam may be used as high-quality fuel, and the high-temperature steam may be guided to a high-temperature regenerator.

Next, the operation will be described. Since the pressure in the dilute solution line L1 is reduced by the pressure reducing valve 17, the regeneration temperature of the dilute solution decreases. As a result, when passing through the intermediate regenerator 18, a part of the dilute solution is vaporized and The liquid flows into the low-temperature regenerator 12 as a two-phase liquid phase. Here, when the dilute solution is vaporized, heat of vaporization (latent heat) is taken from the warm drainage of the exhaust heat line L2.

As described above, since the sensible heat / latent heat exchange moves a large amount of heat as compared with the sensible heat / sensible heat exchange (which is the heat exchange in the prior art), according to the embodiment of FIG. A larger amount of heat is supplied from the heat removal line L2 to the absorption chiller / heater than the heat exchange by the heat source heat exchanger 5 (sensible heat / sensible heat exchange). As a result, the amount of high-quality fuel consumed in the high-temperature regenerator 11 is reduced by an amount corresponding to the increase in the amount of exhaust heat supplied.
% To about 20 to 40%.

Next, the control mode will be described. Here, mode a: high-quality fuel-only operation mode, ie, high-quality fuel-only operation mode, mode b: exhaust heat input and high-quality fuel-fired operation mode, ie, exhaust heat input + high-quality fuel-fired operation mode, mode c: exhaust heat Single input operation mode, that is, exhaust heat single operation mode Thset: Set temperature of hot drainage inlet Tlset: Set temperature of chilled water outlet Tmset: Set temperature of cooling water inlet P: Intermediate pressure, ie, pressure in low-temperature regenerator 12 Tlg: Temperature of low-temperature regenerator 12 Ps: pressure of the dilute solution after exiting the pressure reducing valve 17 Ts: temperature of the dilute solution after exiting the pressure reducing valve 17

FIG. 2 shows a first control mode according to the first and eighth aspects of the present invention. That is, the control unit 30
Are the hot wastewater inlet temperature sensor 33 and the cold water outlet temperature sensor 3
4, the hot water inlet temperature Th and the cold water outlet temperature Tl are detected (step S1), and whether or not the temperature Th is higher than the hot water inlet set temperature Thset, that is, whether the exhaust heat can be input. Is determined (step S
2). If NO, select mode a (step S
3) If YES, it is determined whether the chilled water outlet temperature Tl is higher than the chilled water outlet set temperature Tlset, that is, whether the cooling load is higher than a set value (step S4).
If YES, select mode b (step S5),
If NO, the mode c is selected (step S6).

FIG. 3 also shows a second control mode corresponding to claims 1, 7, 8, and 14. That is, after selecting the mode a in step S3 of the first control mode, a control signal is output to the pressure reducing valve 17, and the optimal solution circulation amount control for the mode a is performed (step SA). Step S5
After selecting the mode b, a control signal is output to the pressure reducing valve 17 to perform the optimal solution circulation amount control for the mode b (step SB). Alternatively, after selecting the mode c in step S6, a control signal is output to the pressure reducing valve 17, and the optimal solution circulation amount control for the mode c is performed (step SC).

FIG. 4 shows a third control mode corresponding to the second and ninth aspects. That is, in addition to the temperatures Th and Tl, the cooling water inlet temperature Tm is detected based on a signal from the cooling water inlet temperature sensor 35 (step S7), and the temperature Th is detected.
Is higher than the temperature Thset, that is, whether or not the exhaust heat can be input is determined (step S8). In the case of NO, the mode a is selected (step S9), and in the case of YES, the pressure P of the low-temperature regenerator 12 changes according to the temperature Tm and the temperature Thset changes. It is determined whether or not it is possible (step S1)
0). If NO, select mode a (step S
9. If YES, it is determined whether the temperature Tl is higher than the temperature Tlset, that is, whether the cooling load is higher than a set value (step S11). If YES, the mode b is selected (step S12) and NO In this case, mode c is selected (step S13). FIG. 5 shows a fourth control mode corresponding to claims 3 and 10. That is, based on the signals from the intermediate pressure sensor 36, in addition to the temperatures Th and Tl, the pressure P in the low-temperature regenerator 12 is detected (step S14). It is determined whether or not it is (step S15). If NO, the mode a is selected (step S16), and YES
Then, it is determined whether the temperature Tl is higher than the temperature Tlset, that is, whether the cooling load is higher than a set value (step S17). If yes, mode b
Is selected (step S18), and if NO, the mode c is selected (step S19).

FIG. 6 shows a fifth control mode corresponding to a combination of the second and third aspects or a combination of the ninth and tenth aspects. That is, the temperature Tm is detected in addition to the temperatures Th, Tl, and the pressure P (step S20), and the pressure P of the low-temperature regenerator 12 changes according to the temperature Tm.
It is determined from the temperatures Th and Tm whether or not the exhaust heat can be input (step S21). If step S21 is NO, mode a is selected (step S22). On the other hand, if YES, in step S23, it is determined whether the chilled water outlet temperature Tl is higher than the set temperature Tlset (ie, whether the cooling load is larger than a set value) (step S23).
23). If step S23 is YES, mode b is selected (step S24), and if NO, mode c is selected.

FIG. 7 shows a sixth control mode according to the fourth or eleventh aspect. In the sixth control mode, the temperature Tl of the low-temperature regenerator 12 is determined based on a signal from the low-temperature regenerator temperature sensor 37 in addition to the temperatures Th and Tl.
g is detected (step S26), and it is detected from the temperatures Th and Tlg whether or not the exhaust heat can be input (step S27).
If step S27 is NO, mode a is selected (step S28). On the other hand, if step S27 is YES, whether temperature Tl is higher than temperature Tlset
That is, it is determined whether the cooling load is larger than the set value (step S29). And step S29 is YE
If S, select mode b (step S30), NO
In the case of, mode c is selected (step S31).

FIG. 8 shows a seventh control mode corresponding to the combination of the second and fourth aspects or the combination of the ninth and eleventh aspects. In the seventh control mode, the temperature Tm is detected in addition to the temperatures Th, Tlg, and Tl (step S32), and it is determined whether the exhaust heat can be input based on the temperatures Th, Tm, and Tlg (step S33). Step S33
Is NO, the mode a is selected (step S3).
4). On the other hand, if YES, the temperature Tl becomes the temperature Tlse
Then, it is determined whether or not the cooling load is greater than the set value (step S35). If step S35 is YES, mode b is selected (step S36), and if NO, mode c is selected (step S37).

FIG. 9 shows an eighth control mode corresponding to the combination of the third and fifth aspects or the combination of the tenth and twelfth aspects. In FIG. 9, the temperatures Th and T
1 and the pressure P, the pressure of the diluted solution after leaving the pressure reducing valve 17 based on the signal from the diluted solution pressure sensor 38 (the low temperature of the pressure adjusting means in the line from the branch of the diluted solution line to the low temperature regenerator). The pressure Ps of the dilute solution on the regenerator side is detected (step S38), and it is determined whether the exhaust heat can be input from the temperature Th and the pressures P and Ps (that is, the intermediate regenerator in consideration of the pressures Ps and P). 18 to determine whether sensible heat / latent heat exchange is possible) (step S39). If step S39 is NO, mode a is selected (step S40). On the other hand, if the exhaust heat can be input (step S
39 is YES), it is determined whether the temperature Tl is higher than the temperature Tlset, that is, whether the cooling load is higher than a set value (step S41). If step S41 is YES, mode b is selected (step S42),
If NO, the mode c is selected (step S43).

FIG. 10 shows a ninth control mode corresponding to a combination of claims 2, 3, and 5, or a combination of claims 9, 10, and 12. That is, the temperature T
The temperature Tm is detected in addition to h, Tl and the pressures P, Ps (step S44), and it is determined from the temperatures Th, Tm, and the pressures P, Ps whether or not the exhaust heat can be input (step S45).
If the determination in step S45 is NO, the mode a is selected (step S46).
Is higher than the temperature Tlset, that is, whether the cooling load is higher than a set value (step S4).
7). If step S47 is YES, mode b
Is selected (step S48), and if NO, the mode c
Is selected (step S49).

FIG. 11 shows a tenth control mode according to the sixth or thirteenth aspect. That is, the temperatures Th, Tl and Ts (the temperature of the dilute solution on the low-temperature regenerator side of the pressure adjusting means in the line from the branch of the dilute solution line to the low-temperature regenerator) and the pressure P are detected (step S5).
0), it is determined whether the exhaust heat can be input based on the temperatures Th and Ts and the pressure P (step S51). Step S51
Is NO, select mode a (step S52),
If YES, it is determined whether the temperature Tl is higher than the temperature Tlset, that is, whether the cooling load is higher than a set value (step S53). If step S53 is YES, mode b is selected (step S5).
4) If NO, select mode c (step S)
55).

FIG. 12 shows an eleventh control mode corresponding to the combination of claims 2, 4, and 6, or the combination of claims 9, 11, and 13. That is, the temperature T
The temperature Tm is detected in addition to h, Tl, Tlg, and Ts (step S56), and it is determined from the temperatures Th, Tlg, Ts, and Tm whether the exhaust heat can be input (step S57).
If step S58 is NO, the mode a is selected (step S58), and if YES, the temperature Tl is reduced to the temperature Tls.
It is determined whether or not the cooling load is larger than the set value (step S59). If step S59 is YES, mode b is selected (step S60), and if NO, mode c is selected (step S61).

FIG. 13 shows an operation control mode (twelfth control mode) in the high-quality fuel-fired single operation, that is, in the mode a. That is, the temperatures Th, Tl, and the like are detected (step S70), and if the operation mode is determined to be mode a by the control mode described with reference to FIG. 2-12 (step S71), the three-way valve 32 for hot drainage is set. , And controls the opening of the three-way valve 32 so that the hot waste water completely bypasses the intermediate regenerator 18 (step S).
72). Then, it is determined whether or not the temperature Tl is higher than the temperature Tlset, that is, whether or not the cooling load is higher than a set value (step S73). Step S73 is YE
If the answer is S, a control signal is output to the fuel control valve 31 to control the opening of the control valve 31 in a direction to increase the supply of high quality fuel to the high temperature regenerator 11 (step S74). The opening of the control valve 31 is controlled in a direction to reduce the supply of high quality fuel.

FIG. 14 shows an operation control mode (thirteenth control mode) in the operation for inputting waste heat and burning high-quality fuel, that is, in mode b. That is, the temperatures Th, Tl, and the like are detected (step S76), and FIG.
If the mode b is determined by the control mode shown in FIG. 2 (step S77), a control signal is output to the three-way valve 32 for hot drainage, and the opening degree of the three-way valve 32 is set so that the hot drainage completely flows through the intermediate regenerator 18. Is controlled (step S78). And
It is determined whether the temperature Tl is higher than the temperature Tlset, that is, whether the cooling load is higher than a set value (step S79). If step S79 is YES, the opening of the fuel control valve 31 is controlled in a direction to increase the supply of high-quality fuel to the high-temperature regenerator 11 (step S80), and NO
In the case of (1), control is performed in a direction to reduce the supply of high-quality fuel (step S81).

FIG. 15 shows a mode of operation control (fourteenth control mode) in an operation mode in which only the exhaust heat is supplied, mode c. That is, the temperatures Th, Tl, and the like are detected (step S82), and if the mode c is determined by the control mode shown in FIG. 2-12 (step S83),
It is determined whether the temperature Tl is higher than the temperature Tlset, that is, whether the cooling load is higher than a set value (step S84). If step S84 is YES, a control signal is output to the hot water drainage three-way valve 32 to control the opening of the three-way valve 32 in a direction to increase the amount of hot water supplied to the intermediate regenerator 18 (step S85), and NO In the case of, the opening degree of the three-way valve 32 is controlled in the decreasing direction (step S8).
6).

FIG. 16 also shows the operation control (fifteenth control mode) in mode c. That is, the temperature Th,
Tl and the like are detected (step S87), and if the mode is determined to be the mode c (step S88), the temperature Tl becomes equal to the temperature Tlse.
Then, it is determined whether or not the cooling load is greater than the set value (step S89). If step S89 is YES, a control signal is output to the hot water drainage three-way valve 32 to control the opening of the three-way valve 32 in a direction to increase the amount of hot water supplied to the intermediate regenerator 18, and to reduce the pressure. A control signal is output to the control unit 17 to control the pressure reducing valve 17 to open (step S90). On the other hand, step S89 is N
In the case of O, the opening of the three-way valve 32 is controlled in a direction to decrease the hot water supplied to the intermediate regenerator 18 and the pressure reducing valve 1
The control is performed in a direction to reduce the number 7 (step S91).

FIG. 17 also shows the operation control (sixteenth control mode) in mode c. First, the temperatures Th and Tl
Are detected (step S92), and the mode c is determined (step S93). Next, the temperature Tl is changed to the temperature Tlse.
It is determined whether or not it is greater than t (step S94).
If S, a control signal is output to the three-way valve 32 for hot drainage,
The three-way valve 32 is fully opened on the side where warm water is supplied to the intermediate regenerator 18 (step S95).
Fully open the three-way valve 32 on the side that bypasses (Step S)
96).

FIG. 18 also shows the operation control (the seventeenth control mode) in the mode c. That is, the temperature Th, Tl, etc. are detected (step S97), and the mode c
Is determined (step S98). Next, it is determined whether the temperature Tl is higher than the temperature Tlset, that is, whether the cooling load is higher than a set value (step S9).
9). If step S99 is YES, a control signal is output to the three-way valve 32 for warm drainage, the three-way valve 32 is fully opened to the side where hot water is supplied to the intermediate regenerator 18, and a control signal is output to the pressure reducing valve 17, Control is performed to open the pressure reducing valve 17 (step S100). On the other hand, if step S99 is NO, control is performed such that the three-way valve 32 is fully closed on the side where the hot water bypasses the intermediate regenerator 18 and the pressure reducing valve 17 is throttled (step S101).

FIG. 19 shows a second embodiment of the present invention, in which the heat source heat exchanger 5 of FIG. 29 is provided between the solution pump P12 of the intermediate concentration solution line L3 and the high temperature solution heat exchanger 14. The same heat source heat exchanger 19 is interposed and connected to the exhaust heat line L2A, and the three-way valve 32A and the temperature sensor 33A
Are connected to the control unit 30, and the other components are configured in the same manner as in FIG. Also in this embodiment, first to first
The control in the control mode 7 is performed, and in the heat source heat exchanger 19, sensible heat / sensible heat exchange is performed between the warm wastewater flowing through the exhaust heat line L2A and the intermediate concentration solution in the intermediate concentration solution line L3. Further, a larger amount of heat can be obtained compared to the embodiment of FIG. 1 by the amount of heat supplied to the absorption chiller / heater by the sensible heat / sensible heat exchange.

FIG. 20 shows a third embodiment of the present invention. In this embodiment, a branch point 16 is provided immediately downstream of the low-temperature solution heat exchanger 15 of the dilute solution line L 1, and an auxiliary line L directly from the branch point 16 to the low-temperature regenerator 12.
The auxiliary line L5 is provided with a heat source heat exchanger 1
9A, and is connected to the exhaust heat line L2B.
And a temperature sensor 33B are connected to the control unit 30, and the other components are configured in the same manner as in FIG. Also in this embodiment, the control in the first to seventeenth control modes is performed, and in the heat source heat exchanger 19A, the warm waste water flowing through the exhaust heat line L2B and the dilute solution flowing through the auxiliary line L5 are separated by sensible heat and heat.
Perform sensible heat exchange. In other words, in the third embodiment, the regenerator 1 is lower than the branch point 16 of the dilute solution line L1.
Exhaust heat is supplied to the absorption chiller / heater by sensible heat / latent heat exchange in the area on the second side, and exhaust heat is supplied by sensible heat / sensible heat exchange on the auxiliary line L5 side.

FIG. 21 shows a fourth embodiment of the present invention, which is an example in which the embodiment of FIG. 19 and the embodiment of FIG. 20 are combined. That is, a heat source heat exchanger 19 is interposed between the solution pump P12 of the intermediate concentration solution line L3 and the high temperature solution heat exchanger 14, connected to the exhaust heat line L2A, and the hot waste water flowing through the exhaust heat line L2A. And intermediate concentration solution line L3
The sensible heat / sensible heat exchange is performed with the intermediate concentration solution.
At the same time, the low-temperature solution heat exchanger 15 of the dilute solution line L1
A branch point 16 is provided immediately downstream of the auxiliary line L5, and an auxiliary line L5 is provided from the branch point 16 directly to the low-temperature regenerator 12, and a heat source heat exchanger 19A is provided in this auxiliary line L5 to provide a heat exhaust line L2B. The sensible heat / sensible heat exchange is performed between the hot waste water flowing through the exhaust heat line L2B and the diluted solution flowing through the auxiliary line L5. Also in this embodiment, the controls in the first to seventeenth control modes are performed, and a larger amount of heat can be obtained than in FIG. 19 or FIG.

FIG. 22 shows a fifth embodiment of the present invention, in which a composite intermediate regenerator 20 in which an intermediate regenerator 20a and a heat source heat exchanger 20b are integrated is provided, and is connected to a waste heat line L2. This is an example in which an intermediate regenerator 20a is interposed in a dilute solution line L1, a heat source heat exchanger 20b is interposed in an auxiliary line L5, and the other components are configured in the same manner as in FIG. Also in this embodiment, the operation is performed in the above-described 1-17th control mode.

In the embodiment shown in FIG. 22, the control of the first to seventeenth control modes is performed. On the intermediate regenerator 20a side of the composite intermediate regenerator 20, the hot drainage of the exhaust heat line L2 and the dilute solution line L1 are controlled. The sensible heat / latent heat exchange is performed with the dilute solution. On the other hand, on the side of the heat source heat exchanger 20b, the waste heat line L
The sensible heat / sensible heat conversion is performed between the hot waste water of No. 2 and the diluted solution of the auxiliary line L5. Also in this embodiment, the operation is performed in the above-described 1-17th control mode.

FIG. 23 shows a sixth embodiment of the present invention, in which a heat source heat exchanger 19 is provided between the solution pump P12 and the high temperature solution heat exchanger 14 of the intermediate concentration solution line L3, Connected to the line L2A,
This is the same as the embodiment. In the embodiment of FIG. 23 as well, the control of the first to seventeenth control modes is performed, and the warm drainage of the exhaust heat line L2A and the intermediate concentration solution of the intermediate concentration solution line L3 performed by the heat source heat exchanger 19 are performed. A larger amount of heat can be obtained than in FIG. 22 by the amount of sensible heat and sensible heat exchange.

The positions a to e described below will be described.

Position a: position of the dilute solution line L1 on the upstream side of the low-temperature solution heat exchanger 15 Position b: position of the dilute solution line L1 between the low-temperature solution heat exchanger 15 and the branch point 16 (FIG. 20) c: Position on the auxiliary line L5 Position d: Position on the auxiliary line L5 on the upstream side of the heat exchanger 19A or 20 Position e: Position on the auxiliary line L5 on the downstream side of the heat exchanger 19A or 20

FIG. 24 shows a seventh embodiment of the present invention, in which the auxiliary heat exchanger 19A is omitted from the auxiliary line L5 in FIG. 20, the three-way valve 21 is provided at the branch point 16, and the positions a to
c, an auxiliary pressure reducing valve 17A (not shown) as a pressure adjusting auxiliary means similar to the pressure reducing valve 17 is provided,
The other is an example configured similarly to FIG. In this form,
By operating both pressure reducing valves 17 and 17A in accordance with the operation mode, the balance between the flow rate and the pressure in the system is adjusted, and the operation is smoothly performed and the heat exchange rate of the exhaust heat is improved. Also in this embodiment, the operation is performed in the above-described 1-17th control mode. However, in the embodiment of FIG. 24, by controlling only the three-way valve 21, it is possible to adjust the balance between the flow rate and the pressure in the system. Alternatively, the pressure reducing valve 17 and the auxiliary pressure reducing valve 17A (provided at any of the positions a to c)
The flow rate / pressure balance can also be controlled by controlling only the two members.

FIG. 25 shows an eighth embodiment of the present invention, in which a three-way valve 21 is provided at a branch point 16 and a position a,
An auxiliary pressure reducing valve 17A is provided in any of b, d and e,
The other is an example configured similarly to FIG. In this form,
The operation is smooth and the heat exchange rate of the exhaust heat is improved. Also in this embodiment, the operation is performed in the above-described 1-17th control mode.

Alternatively, in the embodiment of FIG. 25, it is possible to adjust the balance between the flow rate and the pressure in the system only by the three-way valve 21. Further, the control may be performed using only two members, the pressure reducing valve 17 and the auxiliary pressure reducing valve 17A (not shown).

FIG. 26 shows a ninth embodiment of the present invention, in which a three-way valve 21 is provided at a branch point 16 and a position a,
This is an example in which an auxiliary pressure reducing valve 17A is provided in any of b, d, and e, and the other is configured in the same manner as in FIG. In this embodiment, smooth operation and improvement of the heat exchange rate of the exhaust heat are achieved. Also in this embodiment, the operation is performed in the above-described 1-17th control mode.

In the embodiment shown in FIG.
Or the pressure reducing valve 17 and the auxiliary pressure reducing valve 1
It is possible to perform flow / pressure balance control only with 7A.

FIG. 27 shows a tenth embodiment of the present invention, in which a three-way valve 21 is provided at a branch point 16 and a position a,
This is an example in which an auxiliary pressure reducing valve 17A is provided in any of b, d, and e, and the other is configured in the same manner as in FIG. In this embodiment, smooth operation and improvement of the heat exchange rate of the exhaust heat are achieved. Also in this embodiment, the operation is performed in the above-described 1-17th control mode.

The flow / pressure balance control in the embodiment of FIG. 27 is also performed only by the three-way valve 21 or only by the pressure reducing valve 17 and the auxiliary pressure reducing valve 17A.
You can do it.

FIG. 28 shows an eleventh embodiment of the present invention, in which a three-way valve 21 is provided at a branch point 16 and a position a,
This is an example in which an auxiliary pressure reducing valve 17A is provided in any of b, d, and e, and the other is configured in the same manner as in FIG. In this embodiment, the operation is smoothly performed and the heat exchange rate of the exhaust heat is improved, and the operation is performed in the above-described 1-17th control mode.

In the embodiment shown in FIG. 28, by controlling only the three-way valve 21, or two members of the pressure reducing valve 17 and the auxiliary pressure reducing valve 17A (provided at any of the positions a, b, d and e). By controlling the flow rate in the system,
Pressure balance can be controlled.

[0060]

As described above, according to the present invention,
When a so-called “reverse flow” type absorption chiller / heater is combined with a waste heat source in a cogeneration system or the like, the sensible heat / latent heat exchange with a large amount of heat transfer is performed, so only conventional sensible heat / sensible heat exchange More heat can be supplied from the exhaust heat into the absorption chiller / heater than in the technology of the above. As a result, it is possible to increase the waste heat utilization rate and reduce the consumption of high quality fuel, and approach the target value of 20 to 40%.

Then, the inflow temperature of the fluid supplied from the external heat source, the temperature of the chilled water supplied to the cooling load side, the inflow temperature of the cooling water, the pressure of the low-temperature regenerator or the pressure of the condenser,
According to various operating conditions such as the temperature of the low-temperature regenerator, the pressure or temperature of the dilute solution on the low-temperature regenerator side of the pressure adjusting means, etc., single operation with exhaust heat, single operation with high quality fuel, exhaust heat and high quality Any one of the fuel burning operation modes can be selected. Further, it is possible to adjust the flow rate to the optimum in various operation modes. As a result, optimal control is provided in the operation of the absorption chiller / heater in which very high precision is required for controlling the pressure or flow rate balance.

[Brief description of the drawings]

FIG. 1 is a block diagram showing a first embodiment of the present invention.

FIG. 2 is a flowchart showing a first control mode of the present invention.

FIG. 3 is a flowchart showing a second control mode of the present invention.

FIG. 4 is a flowchart showing a third control mode of the present invention.

FIG. 5 is a flowchart showing a fourth control mode of the present invention.

FIG. 6 is a flowchart showing a fifth control mode of the present invention.

FIG. 7 is a flowchart showing a sixth control mode of the present invention.

FIG. 8 is a flowchart showing a seventh control mode of the present invention.

FIG. 9 is a flowchart showing an eighth control mode of the present invention.

FIG. 10 is a flowchart showing a ninth control mode of the present invention.

FIG. 11 is a flowchart showing a tenth control mode of the present invention.

FIG. 12 is a flowchart showing an eleventh control mode of the present invention.

FIG. 13 is a flowchart showing a twelfth control mode of the present invention.

FIG. 14 is a flowchart showing a thirteenth control aspect of the present invention.

FIG. 15 is a flowchart showing a fourteenth control mode of the present invention.

FIG. 16 is a flowchart showing a fifteenth control aspect of the present invention.

FIG. 17 is a flowchart showing a sixteenth control aspect of the present invention.

FIG. 18 is a flowchart showing a seventeenth control aspect of the present invention.

FIG. 19 is a block diagram showing a second embodiment of the present invention.

FIG. 20 is a block diagram showing a third embodiment of the present invention.

FIG. 21 is a block diagram showing a fourth embodiment of the present invention.

FIG. 22 is a block diagram showing a fifth embodiment of the present invention.

FIG. 23 is a block diagram showing a sixth embodiment of the present invention.

FIG. 24 is a block diagram showing a seventh embodiment of the present invention.

FIG. 25 is a block diagram showing an eighth embodiment of the present invention.

FIG. 26 is a block diagram showing a ninth embodiment of the present invention.

FIG. 27 is a block diagram showing a tenth embodiment of the present invention.

FIG. 28 is a block diagram showing an eleventh embodiment of the present invention.

FIG. 29 is a block diagram showing a conventional absorption chiller / heater.

[Description of Signs] L1, L1A: Dilute solution line L2, L2A: Heat discharge line L3: Intermediate concentration solution line L4: High concentration solution line L5: Auxiliary line 1: Absorption Cold and hot water machine 5 ... Heat exchanger for hot heat source 6 ... Cold water line 7 ... Fuel line 9 ... Evaporator 10 ... Absorber 11 ... High temperature regenerator 12 ... Low temperature regeneration Device 13 ・ ・ ・ Condenser 14 ・ ・ ・ High temperature solution heat exchanger 15 ・ ・ ・ Low temperature solution heat exchanger 16 ・ ・ ・ Branch point 17,17A ・ ・ ・ Reducing valve 18 ・ ・ ・ Intermediate regenerator 19,19A ・..Heat exchanger for heat source 20 ... Compound intermediate regenerator 21 ... Three-way valve 30 ... Control unit 31 ... Fuel control valve 32 ... Three-way valve for hot drainage 33 ... Hot drainage Inlet temperature sensor 34 ・ ・ ・ Cool water outlet temperature sensor 35 ・ ・ ・ Cool water inlet temperature sensor Sensor 36 ・ ・ ・ Intermediate pressure sensor 37 ・ ・ ・ Low temperature regenerator temperature sensor 38 ・ ・ ・ Dilute solution pressure sensor 39 ・ ・ ・ Dilute solution temperature sensor

──────────────────────────────────────────────────続 き Continued on the front page (58) Field surveyed (Int. Cl. ⁶ , DB name) F25B 15/00 303 F25B 15/00 306

Claims (14)

(57) [Claims] 1. A dilute solution line from an absorber to a low temperature regenerator via a low temperature solution heat exchanger, and an intermediate concentration solution line from the low temperature regenerator to a high temperature regenerator via a solution pump and a high temperature solution heat exchanger. Having a pressure adjusting means and an intermediate regenerator between the low temperature solution heat exchanger and the low temperature regenerator of the dilute solution line, the intermediate regenerator is provided with a fluid supplied from an external heat source. Performs sensible heat / latent heat exchange with the fluid in the dilute solution line, and measures the inflow temperature of the fluid supplied from an external heat source. From the output of the chilled water outlet temperature sensor that measures the temperature of the chilled water, the output of the heated effluent inlet temperature sensor, and the output of the chilled water outlet temperature sensor, the operation mode of the absorption chiller / heater can be changed to the high-quality fuel-only operation mode, waste heat input, and Fuel-fired operation mode, exhaust Control means for determining one of the heat only operation modes. 2. The absorption cooling temperature according to claim 1, further comprising a cooling water inlet temperature sensor for measuring a cooling water inflow temperature, wherein said control means also takes in an output of the cooling water inlet temperature sensor as a control element when determining an operation mode. Water machine. 3. An intermediate pressure measuring means for measuring the pressure of the low-temperature regenerator or the pressure of the condenser, wherein the control means also takes in the output of the intermediate pressure measuring means as a control element when determining the operation mode. 2. The absorption chiller / heater of any one of the above. 4. A low-temperature regenerator temperature measuring means for measuring the temperature of the low-temperature regenerator, wherein the control means also takes in the output of the low-temperature regenerator temperature measuring means as a control element when determining an operation mode. 2. The absorption chiller / heater of any of 2. 5. A dilute solution pressure measuring means for measuring a dilute solution pressure on a low temperature regenerator side of a pressure adjusting means interposed in the dilute solution line, wherein the control means performs control when determining an operation mode. 4. The absorption chiller / heater according to claim 3, wherein the output of the dilute solution pressure measuring means is also taken in as an element. 6. A dilute solution temperature measuring means for measuring the temperature of the dilute solution on the low temperature regenerator side of the pressure adjusting means interposed in the dilute solution line, wherein the control means performs control when deciding an operation mode. The absorption chiller / heater according to claim 4, wherein the output of the dilute solution temperature measuring means is also taken in as an element. 7. The absorption chiller / heater according to claim 1, wherein the control means performs a flow rate control optimal for the determined operation mode. 8. A dilute solution line from the absorber to the low temperature regenerator via the low temperature solution heat exchanger, and an intermediate concentration solution line from the low temperature regenerator to the high temperature regenerator via the solution pump and the high temperature solution heat exchanger. In the operation control method of the absorption chiller / heater of the type having, a pressure adjusting means and an intermediate regenerator are interposed between the low-temperature regenerator and the low-temperature solution heat exchanger in the dilute solution line, and the intermediate regenerator is A hot waste water inlet temperature measurement step of performing sensible heat / latent heat exchange between a fluid supplied from an external heat source and a fluid in the diluted solution line to measure an inflow temperature of the fluid supplied from the external heat source And a chilled water outlet temperature measuring step of measuring the temperature of the chilled water flowing from the evaporator to the cooling load side, and changing the operation mode of the absorption chilled and heated water heater to high quality Single burning operation mode An operation mode determining step of determining one of an exhaust heat input and high-quality fuel burning operation mode and an exhaust heat sole input operation mode. 9. The method according to claim 8, further comprising a cooling water inlet temperature measuring step of measuring a cooling water inflow temperature, wherein the operation mode determining step determines an operation mode in consideration of the measured cooling water inlet temperature. Operation control method of absorption chiller / heater. 10. An intermediate pressure measuring step for measuring the pressure of the low-temperature regenerator or the pressure of the condenser, wherein the operation mode determining step sets the operation mode in consideration of the measurement result of the measured intermediate pressure measuring step. The operation control method for an absorption chiller / heater according to any one of claims 8 and 9, wherein the determination is performed. 11. A low-temperature regenerator temperature measuring step of measuring a temperature of the low-temperature regenerator, wherein the operation mode determining step determines an operation mode in consideration of the measured low-temperature regenerator temperature. 9. The operation control method for the absorption chiller / heater according to any one of the above items 9. 12. A dilute solution pressure measuring step of measuring a dilute solution pressure on a low temperature regenerator side of a pressure adjusting means interposed in the dilute solution line, wherein the measured dilute solution is measured in the operation mode determining step. The operation control method for an absorption chiller / heater according to claim 10, wherein the operation mode is determined in consideration of the pressure. 13. A dilute solution temperature measuring step for measuring the temperature of the dilute solution on the low temperature regenerator side of the pressure adjusting means interposed in the dilute solution line, and the dilute solution measured in the operation mode determining step is provided. The operation control method for an absorption chiller / heater according to claim 11, wherein the operation mode is determined in consideration of the temperature. 14. The operation control method for an absorption chiller / heater according to claim 8, further comprising a flow control step of performing a flow control optimal for the determined operation mode.