JPH1114186A - Absorption cogenerating system utilizing engine waste heat and its operation control method - Google Patents

Abstract

PROBLEM TO BE SOLVED: To perform an effective utilization of heat discharged through cooling water or discharged gas outputted from an engine at an absorption cold water or hot water device. SOLUTION: This method is carried out such that hot temperature water 78 heat exchanged with cooling water of an engine 60 is fed into a solution heating means 70, heat is exchanged with solution in an absorption cold water or hot water device 81, further discharged gas 98 of the engine is fed into an auxiliary solution heating means 99 so as to perform a heat exchanging operation with the solution. When an operation aiming at an energy saving of the absorption cold water or hot water device is being carried out, the discharged gas is utilized as a first heat source. In the case that the heating calorie is not enough, the high temperature water is used, and in the case that the heating calorie is further lack, heat is inputted from a burner 25 to a high temperature regenerator.

Description

DETAILED DESCRIPTION OF THE INVENTION

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to an absorption cogeneration system utilizing engine exhaust heat capable of simultaneously performing power generation and cooling and heating, and an operation control method thereof. The present invention relates to an exhaust cogeneration system utilizing an exhaust heat of an engine which is collected and used for cooling and heating, and an operation control method thereof.

[0002]

2. Description of the Related Art An absorption cogeneration system that uses exhaust heat of a power generating engine as a driving heat source for an absorption chiller / heater is disclosed, for example, in Japanese Patent Application Laid-Open No. Hei 7-218017. In this system, hot wastewater and low-pressure steam as exhaust heat from the engine are used as an external heat source for the chiller / heater, and the dilute solution line including the high-temperature solution heat exchanger and the low-temperature solution heat exchanger of the absorption chiller / heater is used. The heat exchange is performed between the dilute solution and the external heat source, and the exhaust heat is effectively used by the absorption chiller / heater.

[0003] Further, assuming that exhaust heat of both engine cooling water and exhaust gas is used, regeneration is performed using hot water obtained by exchanging heat between exhaust gas and water and engine cooling water (jacket hot water). Heating device (Japanese Patent Laid-Open No. 3-12926)
No. 8), in which an exhaust gas boiler is provided and thermally connected to the high-temperature regenerator and the engine cooling water system is thermally connected to the low-temperature regenerator (JP-A-2-130247).
and so on.

[0004]

In the prior art using both the cooling water and the exhaust gas as described above, the absorbing solution is disposed in an exhaust heat high-temperature regenerator using exhaust heat as a driving source and a direct-fired high-temperature regenerator using a burner. Are not considered.

An object of the present invention is to heat a dilute solution with engine cooling water, use an exhaust gas high-temperature regenerator using exhaust gas as the exhaust heat high-temperature regenerator, and further use the exhaust hot water, exhaust gas, and direct combustion. An object of the present invention is to provide an absorption-type cogeneration system in which the amount of supplied fuel is controlled based on the temperature and pressure of each part, and which is efficient, safe, and excellent in startup characteristics.

[0006]

In order to achieve the above object, the present invention provides at least a high-temperature regenerator, a low-temperature regenerator,
An absorption chiller / heater equipped with a condenser, an evaporator, an absorber, a low-temperature heat exchanger, and a high-temperature heat exchanger as components; high-temperature water generated by cooling a jacket of a generator driving engine; Solution heating means for performing heat exchange with the solution of the cycle flowing through, high-temperature water circulation means for circulating the high-temperature water to the solution heating means, exhaust gas of the engine and the inside of the absorption cold water heater. Auxiliary solution heating means for performing heat exchange with the solution of the flowing cycle, exhaust gas introduction means for flowing the exhaust gas through the auxiliary solution heating means, and a burner provided in the high temperature regenerator A fuel control means for controlling a fuel supply amount of the hot water; a high-temperature water circulation amount control means for controlling a circulation amount of high-temperature water circulated to the solution heating means; That discloses an exhaust gas flow amount control means for controlling the flow amount of the exhaust gas, the engine exhaust heat utilization absorption cogeneration system, comprising a.

Further, the present invention provides the above-mentioned absorption cogeneration system utilizing the exhaust heat of the engine, wherein the auxiliary solution heating means is provided between the dilute solution from the high temperature heat exchanger to the high temperature regenerator and the high temperature water. Disclosed is an engine waste heat absorption cogeneration system arranged to perform heat exchange.

The present invention also relates to the above-mentioned absorption cogeneration system utilizing engine exhaust heat, wherein the dilute solution flowing out of the high-temperature heat exchanger of the absorption chiller / heater is divided into two parts, and one of the two is heated and concentrated by a high-temperature regenerator. And an absorption type cogeneration system utilizing engine exhaust heat, wherein the other is heated and concentrated by the auxiliary solution heating means.

Further, the present invention provides the above-mentioned cogeneration system utilizing the exhaust heat of the engine, wherein the auxiliary solution heating means exchanges heat between the solution concentrated in the high temperature regenerator and the high temperature water. An absorption cogeneration system utilizing exhaust heat of an engine, wherein the cogeneration system is arranged to perform the operation.

Further, the present invention relates to an operation control method of the above-mentioned cogeneration system utilizing the exhaust heat of an engine,
First calculating means for calculating a required cooling and heating capacity required for the absorption chiller / heater, and high-temperature water heating amount which can be taken into the solution cycle of the absorption chiller / heater from the high-temperature water by the solution heating means. And second computing means for calculating an exhaust gas heat amount that can be taken into the solution cycle from the exhaust gas by the auxiliary solution heating means. Priorities for using the exhaust gas, high-temperature water, and burner as heat sources for realizing the required cooling and heating capacity calculated by the first calculating means are determined in advance, and the required cooling and heating capacity, the high-temperature water heating amount, The fuel control unit, the high-temperature water circulation amount control unit, and the exhaust gas flow rate control unit based on the relationship between the magnitude of the heat quantity of the exhaust gas and the priority. It discloses a driving control method characterized by controlling the operation.

[0011]

Embodiments of the present invention will be described below. FIG. 1 is a system diagram showing an example of a configuration of an absorption type cogeneration system according to the present invention.
1. A power generation module 80 having a control panel 62, an exhaust heat utilizing absorption chiller / heater 82 having an absorption chiller / heater 81 having a solution heating means 70 and an auxiliary solution heating means 99, and an air conditioner 8
5, a cooling tower 87, a radiator 64, and the like.
The power generation module 80 is supplied with intercooler cooling water for cooling air compressed by the turbocharger, fuel and air for the engine, auxiliary commercial power for security equipment, etc., to generate power and to generate high-temperature exhaust gas from the exhaust duct. Is discharged, and the jacket cooling water 63 of the engine 60 is discharged as high-temperature water 78 via the high-temperature water heat exchanger 68. On the other hand, in the exhaust heat utilizing absorption chiller / heater 82, fuel is supplied to the burner 25 via the fuel control means 26,
The solution is burned in the combustion chamber 29 to heat the solution in the high-temperature regenerator.
The high-temperature water 78 from the power generation module 80 flows through the solution heating means 70 via the high-temperature water introduction conduit 71 by the high-temperature water circulation amount control means 77, and heats the solution in the absorption cycle to give thermal energy. Further, the exhaust gas 98 from the power generation module 80 is supplied to the exhaust gas
The solution is sent to the auxiliary solution heating means 99 via 0, and heats the solution in the absorption cycle to give thermal energy. The cold / hot water 83 generated by the exhaust heat utilization absorption chill / hot water machine 82 is sent to the air conditioner 85 by the cold / hot water circulation means, and is used for cooling and heating.
Of course, the same function can be exerted by using a latent heat medium such as a high-pressure refrigerant instead of the cold / hot water 83.

Next, referring to FIG.
2 will be described. First, the absorption chiller / heater comprises a high-temperature regenerator 1, a low-temperature regenerator 2, a condenser 3, an evaporator 4, an absorber 5, a low-temperature heat exchanger 6, a high-temperature heat exchanger 7, a solution circulation pump 8, a refrigerant spray pump 9 , A solution spray pump 10 and the like. In addition, a solution heating means 70 for heating the solution with the high-temperature water 78 and an auxiliary solution heating means 99 for heating the solution by exchanging heat with the engine exhaust gas 98 are arranged to constitute a waste heat utilizing absorption chiller / heater 82. is there.

Next, the cooling operation of the exhaust heat utilizing absorption chiller / heater 82 will be described. The dilute solution having a low lithium bromide concentration in the high-temperature regenerator 1 is heated by the combustion gas of the burner 25 (FIG. 1), boiled to generate refrigerant vapor, and concentrated.
The steam generated in the high-temperature regenerator 1 passes through the eliminator 30a and exchanges heat with the dilute solution flowing down the outside of the heat transfer tube of the low-temperature regenerator 2 to be condensed and liquefied. Flows into. The solution heated by the low-temperature regenerator 2 generates a refrigerant vapor and becomes a concentrated solution. The vapor generated by the low-temperature regenerator 2 is supplied to an eliminator 30 serving as a solution mist removing means.
The cooling water 86 flows into the condenser 3 via the b and is cooled by the cooling water 86 flowing in the heat transfer tube to be condensed and liquefied. The refrigerant liquid generated in the condenser 3 is stored in a refrigerant liquid tank 21a and passes through a refrigerant flow control valve 13 which is a refrigerant flow control means.
Flows into. The refrigerant liquid in the refrigerant liquid tank 21b at the lower part of the evaporator 4 is cooled by a refrigerant spray pump 9 into a refrigerant spraying means 20.
Is cooled on the evaporator heat transfer tube group, and cools the cold water flowing in the tubes to evaporate. At this time, the latent heat of evaporation is removed from the cold water to exert a cooling effect. On the other hand, the concentrated solution generated in the high-temperature regenerator 1 overflows into the float box 34, passes through the high-temperature heat exchanger 7, and the diaphragm 15 and the low-temperature regenerator 2
And the concentrated solution from the low-temperature regenerator 2 via the self-evaporator 35 connected to the gaseous phase section, and the solution spray pump 10 guides the concentrated solution to the absorber 5 via the low-temperature heat exchanger 6 to spray the solution. Sprayed on the absorber heat transfer tube group by the means 19, cooled by the cooling water 86 flowing through the tubes, and absorbed and diluted by the refrigerant vapor from the evaporator 4. The dilute solution generated in the absorber 5 falls into the dilute solution tank 22, is sent out by the solution circulation pump 8, is heat-exchanged with the concentrated solution in the low-temperature heat exchanger 6, is preheated, is divided into two, and one is at low temperature. It is sent to the regenerator 2. The other is heated by the high-temperature water 78 in the solution heating means 70, and is further preheated by exchanging heat with the concentrated solution in the high-temperature heat exchanger 7.
It is guided to the auxiliary solution heating means 99 via the high temperature regenerator solution circulation amount control means 14 disposed in the inside 4, is heated by exchanging heat with the engine exhaust gas 98, flows into the high temperature regenerator 1 and makes a round. .

As described above, the exhaust heat-utilizing absorption chiller / heater 82 uses the heat energy of the exhaust gas 98 of the engine 60,
Utilizing a part of the heat energy of the jacket cooling water 63,
It constitutes a double effect parallel flow absorption refrigeration cycle. According to this configuration, heat exchange is performed between the dilute solution flowing into the high-temperature regenerator 1 and the exhaust gas 98. However, since the boiling point of the dilute solution is low and the heat exchange temperature difference can be increased,
The heat exchanger can be miniaturized or the exhaust heat utilization rate can be increased, and the exhaust gas temperature can be lowered.

Next, the heating operation of the absorption chiller / heater 82 utilizing exhaust heat will be described with reference to FIG. During heating, the cooling / heating switching valve 11 is opened, and the steam generated by the high-temperature regenerator 1 is introduced into the shells of the evaporator 4 and the absorber 5, and heats the hot water flowing through the heat transfer tubes of the evaporator 4 to condense and liquefy. , Falls into the refrigerant liquid tank 21b. The refrigerant liquid in the refrigerant liquid tank 21b is:
The refrigerant is discharged to the absorber 5 via a refrigerant pump 9 and a refrigerant blow valve 12 which are refrigerant liquid discharge means of the refrigerant liquid tank. The refrigerant liquid that has flowed into the absorber 5 mixes with the solution to form a dilute solution, which is sent out by the solution circulation pump 8 and is supplied to the low-temperature heat exchanger 6.
Is pre-heated by heat exchange with the concentrated solution, is divided into two, and one is sent to the low-temperature regenerator 2. The other is a solution heating means 7
0, and is preheated by exchanging heat with the concentrated solution in the high-temperature heat exchanger 7, and the auxiliary solution is heated through the high-temperature regenerator solution circulation amount control means 14 disposed in the float box 34. The heat is exchanged with the engine exhaust gas 98, heated by the means 99, flows into the high-temperature regenerator 1, and reheated by the combustion heat of the burner 25 to generate refrigerant vapor. 5 constitutes a cycle of flowing into the shell 5 via the cooling / heating switching valve 11. On the other hand, the concentrated solution in the high-temperature regenerator 1 overflows into the float box 34 and passes through the high-temperature heat exchanger 7 to
The solution from the low-temperature regenerator 2 is merged with the solution from the low-temperature regenerator 2 via the self-evaporator 35 connected to the gas phase of the low-temperature regenerator 2, and guided to the absorber 5 via the low-temperature heat exchanger 6 by the solution spray pump 10, The solution is sprayed onto the absorber heat transfer tube group by the solution spraying means 19, flows down, and mixes with the liquid refrigerant from the refrigerant liquid tank 21b of the evaporator 4 to become a dilute solution. At this time, in the low-temperature regenerator 2, the solution simply circulates. The refrigerant liquid in the refrigerant liquid tank 21a is sent to the evaporator 4 by opening the refrigerant flow control valve 13 and sent to the absorber 5 by the refrigerant pump 9 via the valve 12 to reduce the solution concentration in the cycle. doing. As described above, even in the case of heating, the exhaust-heat-use absorption chiller / heater 82 partially utilizes the heat energy of the exhaust gas 98 of the engine 60 and the heat energy of the jacket cooling water 63 to perform the dual-effect parallel flow absorption and heating cycle. Is composed.

As described above, in the present invention, not only the cooling water of the engine jacket but also the exhaust heat of the exhaust gas is utilized to increase the efficiency of the absorption chiller / heater. An operation control method for making the above more effective will be described below. FIG. 3 is a flowchart showing the operation control method, which is cyclically executed by the control panel 32 of FIG. 2 at a predetermined cycle.

First, when the air conditioner 85 is operated and the operation switch of the absorption chiller / heater is turned on, the power generation module 80 is turned on.
It is checked whether or not is operated (step 301). For this check, the power generation module 8
When 0 is operated and the engine 60 is operated, a high pulsating wind pressure of a level of 1 kPa is applied to the exhaust duct, and this is detected by the pressure sensor 115 and used as an operation signal of the power generation module 80. Alternatively, the temperature of the exhaust gas may be detected by a thermometer provided in the exhaust gas duct, and the determination may be made based on whether the temperature exceeds a predetermined value. According to these methods, it is not necessary to exchange signals between the control panel 62 of the power generation module 80 and the operation control panel 32 of the chiller / heater, and the configuration can be simplified. As a result of the above check, if the engine 60 of the power generation module 80 is not operating, the operation enters the absorption chiller / heater single operation mode. That is, the high-temperature water circulation amount control unit 77 is controlled so that high-temperature water is not sent to the solution heating unit 70. Similarly, the exhaust gas flow control means 100 is controlled so that the exhaust gas does not flow through the auxiliary solution heating means 99 but is sent to the exhaust gas bypass duct 114.
As a result of the check in step 301, the power generation module 80
When it is determined that the engine 60 has been operated,
The operation mode is changed to the absorption chiller / heater exhaust heat utilization operation mode. That is, the flow rate of the heat charge to the burner 25 is controlled by comparing the cooling / heating load condition with the amount of heat that can be recovered from the exhaust gas and the high-temperature water. Hereinafter, the operation of the absorption chiller / heater exhaust heat utilization operation mode will be described.

In this operation mode, first, a cooling / heating load, that is, a required cooling / heating capacity QH required at present is estimated from the cooling / heating water data of the absorption chiller / heater and the target setting value of the cooling / heating water temperature (step 302). For this, first, the cold / hot water 83 detected by the temperature sensors 89 and 90 is used.
Temperature tEW1, outlet temperature tEW2 and cold and hot water flow rate WE
And from

## EQU1 ## The current cooling / heating capacity (output) is obtained from QE = CE.WE (tEW1-tEW2) (CE is a constant). Here, in the case of a system in which the flow rate of the chilled / hot water is made variable, the information of the chilled / hot water flow rate WE is obtained from the detected value of the cold / hot water inlet / outlet differential pressure △ PEW of the evaporator 4, for example.
Can be estimated using the fact that is proportional to the (（) power of the differential pressure △ PEW. Further, a temperature difference between the above inlet temperature tEW1 and the set water temperature tEW10.

２tE = tEW1−tEW10 is obtained, and a value T minutes after the value (T: about several minutes) is also obtained as △ tET, and a time change rate of the temperature difference is obtained.

## EQU3 ## η = (△ tE- △ tET) / T is obtained. ΔtE is a positive value during cooling and a negative value during heating, and the larger the absolute value is, the more heat input is required to achieve the set temperature.
Is a value for predicting a change in the additional heat quantity. Then, using the coefficients α and β of the control elements determined in the same manner as the proportional and differential control in the normal control system,
From equation (3), the required additional cooling / heating capacity △ QE

△ QE = α · △ tE + β · η Therefore, the required cooling / heating capacity QH of the absorption chiller / heater as a whole is

## EQU5 ## It is obtained by QH = QE + △ QE.

The required cooling / heating capacity QH cannot be used as it is for controlling the actual output. That is, the heat cycle of the absorption chiller / heater has a maximum heat input limit QHmax. This is the limit where the steam flow rate in each part of the cycle exceeds the limit value and gas-liquid separation becomes insufficient when heat input is applied any more, or trouble occurs or the operating pressure exceeds the atmospheric pressure Or the safety devices are activated and the operation is not continued. Therefore (Equation 5)
Even if the value exceeds QHmax, the heat quantity cannot be given to the cycle, so that QH in (Equation 5) must be set to the following value.

## EQU6 ## QH = min (QE + △ QE, QHmax)

In the next step 303 of FIG. 3, the maximum amount of heat that can be taken from the high-temperature water 78 under the engine operating condition at that time, that is, the high-temperature water heat amount QW is calculated. The hot water heating value QW is generally given by the following equation:

(Equation 7) Here, Th1 is the inlet temperature of the high-temperature water solution heating means 70,
T1 is the inlet temperature of the solution, and gW is the flow rate of the high-temperature water (the maximum flow rate available in the solution heating means). Step 3
At 04, the maximum heat quantity that can be taken from the exhaust gas 98 under the engine operating state at that time, that is, the exhaust gas heat quantity QG is calculated. This QG is similar to the case of hot water

(Equation 8) Given by Here, Th2 is the inlet temperature of the exhaust gas to the auxiliary solution heating means 99, T2 is the inlet temperature of the solution, and gG is the flow rate of the exhaust gas output from the engine (the maximum flow rate usable by the auxiliary liquid heating means). . Also, fw, fG
Is a function using the value in parentheses as a variable, which are measured in advance as characteristics of the solution heating means 70 and the auxiliary solution heating means 99 and are obtained in the form of a table. In either solution heating means, as shown in (Equation 7) and (Equation 8), when the inlet temperature of the high-temperature water or the exhaust gas is equal to or lower than the solution temperature of the solution heating means, the heating amount is set to 0. I do.

Of the variables in (Equation 7) and (Equation 8), the temperature T of the solution at the inlet of each solution heating means 70 and 99
1 and T2 are detected by temperature sensors 79 and 118 installed to measure the respective values. On the other hand, there are several methods for detecting the inlet temperatures Th1, Th2 and the flow rates gW, gG of the high-temperature water and the exhaust gas. At least each of the inlet temperatures Th1, Th2 is compared with the solution temperatures T1, T2, respectively. Since it is necessary to determine whether or not to operate each solution heating means, these temperatures T1 and T2 must be measured directly. Therefore, the temperature sensors 76 and 11
6 are installed. For the flow rates gW and gG,
Again, these can be detected directly. That is, the flow rate gW of the high-temperature water is determined by the high-temperature water circulation means 72 (FIG. 1).
It can be easily understood from the operation state of. On the other hand, the exhaust gas flow rate gG
Can be easily estimated from the pressure detected by the pressure sensor 115 provided at the exhaust gas inlet. In this direct method, all the amounts required for calculating the amount of heat can be obtained from the sensors in the waste heat utilizing absorption chiller / heater 82.

Further, in the gas engine for power generation, the relationship between the value of the input (flow rate or output (power) of the heat quantity for power generation), the temperature and flow rate of the exhaust gas, and the required heat radiation amount of the high-temperature water is measured in advance. Since these data are given, the function fW1 directly relating the input Pin or output Pout of the engine to the high-temperature water heat quantity QW and the exhaust gas heat quantity QG from these data and the functions fW and fG of (Equation 7) and (Equation 8). , FG1;

## EQU9 ## QW = fW1 (Pin or Pout) QG = fG1 (Pin or Pout) may be prepared in a table format in advance. FIG.
Shows an example of the high-temperature water heat quantity QW and the exhaust gas heat quantity QG with respect to the engine input Pin obtained as described above. In this method, it is necessary to take the value of the input Pin or the output Pout of the engine from the power generation module 80 into the control panel 32 of the exhaust heat utilizing absorption chiller / heater 82.

As described above, the required cooling / heating capacity QH required for the absorption chiller / heater, the amount of heat from the high-temperature water available under the engine operating state at that time, that is, the high-temperature water heating amount QW and the exhaust gas Is calculated, that is, the amount of heat applied to the exhaust gas QG is calculated, and then the flow rate control of the high-temperature water 78 and the exhaust gas 98 flowing to the solution heating means 70 and the auxiliary solution heating means 99 is performed based on these data. However, for this purpose, it is necessary to arrange the relationship between the cooling and heating capacity of the absorption chiller / heater and the amount of heat input from the burner, the solution heating means, and the auxiliary solution heating means. Table 1 shows the relationship between the heat energy input from each heat source during the cooling operation and the conversion of the heat energy to the cooling capacity by the absorption refrigeration cycle, and the cooling capacity exerted by the heat energy of the combustion gas of the burner 25. The standard conversion calorie of each heat source heat energy,
In other words, it represents the contribution of saving heat input to the burner 25 by the heat recovery location.

[Table 1]

The heat energy PB input by heating the burner 25 with the combustion gas is given to the high-temperature regenerator 1 and converted into a cooling capacity QHB by an absorption refrigeration cycle. The conversion coefficient at this time is a so-called coefficient of performance (COP),
Let it be C0. When heat is recovered from high-temperature water by the solution heating means 70, the contribution to the cooling capacity differs depending on the absorption refrigeration cycle, and the conversion coefficient is C1. Therefore, the amount of heat PW recovered by the solution heating means 70 saves the amount of heat given to the high temperature regenerator 1 by the combustion gas from the burner 25 by (C1 / C0) PW. Further, when heat is recovered from exhaust gas by the auxiliary solution heating means 99, the effect is almost the same as that of the high-temperature regenerator 1, and the conversion coefficient may be C0. Therefore, the heat amount PG recovered by the auxiliary solution heating means 99 saves the heat amount given by the combustion gas from the burner 25 to the high temperature regenerator 1 by PG.

The above is the case of cooling. However, in the case of heating, the coefficients of performance shown in Table 1 are all equal from each other due to the heat cycle configuration, and this is referred to as C0. However, the value of C0 at the time of heating is not the same as the value of C0 at the time of cooling, but the same symbol is used for simplicity.

Returning to FIG. 3, the burner combustion amount,
The actual flow control of the high-temperature water and the exhaust gas will be described. The basis of this control is a heat input amount P from each heat input source shown in Table 1.
B, PW, and PG to control the sum of the cooling / heating capacity to be the required cooling / heating capacity QH obtained in (Equation 6) above;

QH = QHB + QHW + QHG Furthermore, in order to satisfy this condition, the heat quantity of high-temperature water and exhaust gas is used preferentially, and even if heat is insufficient, heat is input from the burner, and waste heat is used as efficiently as possible. I do.

For this purpose, first, step 305 in FIG.
so,

It is checked whether QH> QHBmin + C1.QW + C0.QG holds. Where QHBmin is the burner 2
Assuming that the minimum heat input that can be burned in 5 is PBmin

## EQU12 ## This is a constant given by QHBmin = C0.PBmin. (Equation 11) holds because
Even if all the available heat inputs QW and QG from the high-temperature water and exhaust gas are used, the minimum heat input PBmin from the burner 25 is obtained.
This means that the above input is required. So at this time

## EQU13 ## The burner 2 is arranged so that the heat quantity PB = QH / C0- (C1 / C0) QW-QG is output from the burner.
5 is performed (step 305). However, since the amount of heat that can be output from the burner 25 is limited, if the maximum value is PBmax, (Equation 13) needs to be as follows;

PB = min (QH / C0- (C1 / C0) QW-QG, PBmax)

In the next step 306,

It is assumed that PW = QW PG = QG. Here, PW = QW means that the high-temperature water circulation amount control means 77 is controlled so that all of the high-temperature water 78 passes through the solution heating means 70, and at the same time, the high-temperature water bypass means 74 is controlled so that the high-temperature water In order to prevent the heat radiation here from occurring, so as to utilize the entire available heat amount QW from the high-temperature water. However, as described in (Equation 7), if the inlet temperature Th1 of the high-temperature water is lower than the inlet temperature T1 of the solution, heat is taken from the solution toward the high-temperature water. Therefore, when QW = 0, high-temperature water is not passed through the solution heating means 70, and heat is radiated by the radiator 64.

The meaning of PG = QG in (Equation 15) is the same as in the case of high-temperature water. If QG> 0, the gas flow rate control means 100 is controlled to exhaust gas exhaust gas and the auxiliary solution heating means 99 And exhaust gas heat quantity QG available from exhaust gas is used. However, the exhaust gas inlet temperature Th2
Is lower than the solution inlet temperature T2, QG = 0. At this time, the exhaust gas is not passed through the auxiliary solution heating means 99.

If the condition of (Equation 11) is not satisfied in the judgment of step 305, PB = 0, that is, the burner 25
Is stopped (step 307). This is because at least the amount of heat required for the burner 25 is small, which means that the amount of heat input is equal to or less than the minimum heat input PBmin. And then

## EQU16 ## C1 · QW + C0 · QG <QH (≦ QHBmin + C1
(QW + C0.QG) is checked (step 308). If this condition is satisfied, it is necessary to use all of the available heat amounts QW and QG from the high-temperature water and the exhaust gas. However, when the condition of (Equation 16) is not satisfied,

It is checked whether or not C0 · QG <QH (≦ C1 · QW + C0 · QG) holds (step 309). This condition is satisfied when the required cooling / heating capacity QH is C1 · QW + C0 · Q
Since it is smaller than G, but larger than the contribution QHG from the heat quantity of exhaust gas C0 · QG, introduction of the high-temperature water to the solution heating means 70 is stopped, and heat radiation of the high-temperature water is performed by the radiator 64 ( PW = 0), exhaust gas is introduced into the auxiliary solution heating means 99 (step 310). Of course, when the exhaust gas inlet temperature Th2 is lower than the solution inlet temperature T2, that is, when QG = 0, the exhaust gas is not introduced. If the condition of step 309 is not satisfied, the state where neither high-temperature water nor exhaust gas is used, that is, PW = PG = 0 is set (step 311).

As described above, in the operation control method shown in FIG. 3, the required cooling / heating capacity QH calculated in step 302 is realized by using exhaust heat of exhaust gas and high-temperature water as much as possible. Since it is controlled so that heat input from the burner is performed only when the operation is performed, economical operation becomes possible. In step 305, the combustion of the burner 25 is continuously controlled in accordance with the required amount. The flow rate control of the high-temperature water and the exhaust gas is performed by using all the available heat amounts QW and QG or setting them to zero. Step 3 on / off control
06, 310, and 311. This has a feature that the control system is simplified and an economical configuration is possible.

Next, a modification of the flow shown in FIG. 3 will be described. First, in step 310, the control for setting PW = 0 is changed. When the process proceeds from step 309 to step 310, the condition of step 308 (expression 16) is not satisfied, and the condition of step 309 (expression 17) is satisfied.

## EQU18 ## C0.QG <QH.ltoreq.C1.QW + C0.QG. Therefore, if a quantity of heat corresponding to QH-C0.QG (.ltoreq.C1.QW) is taken from the high-temperature water, a smoother temperature control than the above-mentioned on / off control becomes possible. Therefore, as a first modification, the control in step 310 of FIG.

PW = QH / C0− (C1 / C0) · QG It is assumed that PG = QG. Here, the first expression of (Equation 19) means the following control. First, with respect to the maximum flow rate of the high-temperature water qW and the high-temperature water heat quantity QW, when the flow rate is pW, the heat quantity actually input to the cycle from the solution heating means 70 is proportional to the flow rate.
QW / qW. Accordingly, the flow rate pW at which this value becomes equal to the right side of the first equation of (Equation 19);

The opening degree of the high-temperature water circulation amount control means 77 is analogously controlled so that the high-temperature water of pW = (QH / C0- (C1 / C0) .QG) (qW / QW) flows to the solution heating means 70. (Equation 19) is the meaning of the first equation. However, when QW = 0, PW =
O is the same as in step 306. According to this modification, the temperature control becomes smoother than the on / off control of FIG. 3, and the comfort increases.

A second modification of the flow of FIG.
In step 11, the control for setting PG = O is changed. In step 311, since (Equation 17) is not satisfied,

The control is performed such that PW = 0 and PG = QH / C0. For this purpose, for the maximum flow rate qw of the exhaust gas and the heat quantity QG of the exhaust gas,

The opening degree of the exhaust gas flow rate control means 100 may be controlled in an analog manner so that the flow rate pG of pG = (QH / C0). (QG / QG) flows to the auxiliary solution heating means 99. In this case, the required cooling / heating capacity QH ≦
Needless to say, when 0 or the exhaust gas heat amount QG = 0, PG = pG = 0 so that the exhaust gas is not used. As described above, the same effect as the first modification can be obtained by using the heat input from the exhaust gas in an analog manner. Further, if the first modification is combined with the second modification described above, that is, the heat input amount PW from the high-temperature water is analogously controlled in step 310 of FIG. If the amount of heat PG is controlled in an analog manner, smoother and more comfortable temperature control can be achieved.

FIG. 4 shows a third modification of FIG. This figure 4
3 is a modification of the steps 307 to 309 in FIG. 3 as in steps 407 and 408. The burner 25 performs an operation control method for controlling at least the minimum possible combustion amount to always burn. Is shown. That is, first, when the condition of step 305 shown in (Equation 11) is satisfied, it is the same as in FIG. 3, and all the available heat amounts QW and QG from the high-temperature water and the exhaust gas are used, and the shortage is used. Heat is input from the burner (Step 30)
5, 306). On the other hand, when the condition of step 305 is not satisfied, PB = PBmin, that is, the burner is burned with its minimum combustion amount (step 407). And conditions

## EQU23 ## It is checked whether or not QH-QHBmin> C0.QHG is satisfied (step 408). If it is satisfied, the exhaust gas heat amount QG is used entirely and high-temperature water is not used (step 310). If the condition of step 408 shown in (expression 23) is not satisfied, the heat input from the exhaust gas is also stopped (step 311).

According to the operation control method shown in FIG. 4, the burner always burns at least for its minimum combustion amount. In general, the burner performs pre-barge every time it ignites and post-purges each time it extinguishes the fire, so that air flows through the combustion chamber in the high-temperature regenerator 1. Therefore, heat loss occurs from the heated solution. According to the control method, by maintaining the minimum combustion state, the heat dissipation loss as described above can be significantly reduced, and this is particularly effective for energy saving in the middle season such as spring and autumn when the heat load is small.

In FIG. 4, the use of the exhaust heat of the high-temperature water and the exhaust gas is based on the on / off control as shown in steps 310 and 311. However, as described in the first and second modifications of FIG. Alternatively, one or both of the exhaust heat may be controlled in an analog manner instead of the on / off control. In this case, a more comfortable temperature control effect can be obtained.

The operation control method based on FIG. 3 or FIG. 4 and the modifications thereof has been described above.
As an operation control method in consideration of safety and safety, there is a method in which a heat input limit QHmax to the absorption chiller / heater and a solution circulation amount in a cycle are made variable. These control methods are known as absorption chiller / heater control methods, but their effects can be further exhibited by applying to the cogeneration system of the present invention.

First, the heat input limit QHmax is in a temperature range where the solution temperature THG of the high-temperature regenerator 1 is within a certain range, for example, 80 ° to 160 ° C.
In the range, the heat input limit QHmax is set larger, and when the temperature is higher or lower than that range, the heat input limit QHmax is set smaller. When the cooling water temperature Twci is high, the heat input limit QHmax is set small. The reason why the heat input limit QHmax is reduced when the temperature THG or Twci is low is that it occurs at the start of operation or the like. However, since the pressure of the high-temperature regenerator 1 is low, the boiling heat transfer coefficient is low, and The temperature difference between the hot surface and the liquid becomes large, so that corrosion deterioration is likely to occur. Also, when the solution temperature of the high-temperature regenerator is high, corrosion deterioration is apt to occur due to the rise of the heat transfer surface temperature. Therefore, the heat input limit QHmax is made small to reduce the heat exchange temperature difference, thereby preventing this corrosion. When controlling the heat input limit QHmax, the same control can be performed by using the solution temperature TLG of the low-temperature regenerator 2 instead of the solution temperature THG of the high-temperature regenerator 1.

Next, control of the solution circulation amount in the cycle will be described. This control is based on the solution outlet temperature of the low-temperature regenerator 2,
The condensing temperature at which the refrigerant generated from the high-temperature regenerator 1 is condensed and liquefied in the heat exchanger of the low-temperature regenerator 2, the temperature of the evaporator 4, the temperature of the solution outlet of the absorber 5, the condensing temperature of the condenser 3, the high-temperature regenerator Cycle calculation is performed by estimating the solution temperature of each part by a known method from the temperature (THG) and the like in accordance with the During relation, and the amount of solution circulation for realizing a high efficiency cycle is calculated. In comparison, the solution circulation pump 8
An optimum cycle is realized by controlling the number of rotations of the solution spray pump 10. Two different purposes can be set for this control. That is, 1) an operation mode in which energy saving by using exhaust heat is emphasized and the exhaust heat of the gas engine 60 is used. 2) An operation mode in which the comfort of cooling and heating is emphasized and the target cooling and heating capacity is exhibited as soon as possible. Of these, 1) is operated so that the cold water temperature is as high as possible or the hot water temperature is as low as possible. That is, in the operation mode 1), the chilled water set temperature during the cooling operation is automatically set to about 2 degrees higher, and the hot water temperature during the heating operation is set to 5 degrees.
Be sure to set the temperature at a low temperature. In the case of 2), the time delay of the heat input is calculated, and the heat source with a quick response, that is, the exhaust gas heat utilization is emphasized. Then, the reheating gas burner is used, and the use of the high-temperature water with a slow response is later. . Therefore, even when the engine 60 is operating, the reburning burner 25 is operated earlier than the high-temperature water use. In the operation control method shown in FIG. 3 or FIG. 4, from the viewpoint of effective use of exhaust heat, when the required cooling / heating capacity QH is small, first the exhaust gas, then the high-temperature water, and then, if a larger heat input is required, the burner. Although the heat source was used, it is easy to change the order according to the purpose. Case 2) corresponds to the case where the order of using the high-temperature water and the burner in FIGS. 3 and 4 is changed.

In the above two operation modes, load conditions for several days are stored, and prediction control is performed by automatically switching from the load pattern and the weather condition of the day, for example, the outside temperature, atmospheric pressure, wind speed, humidity, and the like. It is desirable to switch to the operation mode 1) especially in a relatively comfortable situation where the outside air is cool and the breeze is blowing during cooling. In addition, when it is hot and humid, or when the solar radiation is severe, the operation mode is switched to the operation mode 2). In addition, when heating, the outside temperature is low,
If the wind is strong, switch to 2), and switch to 1) because the weather becomes warm during the day. As described above, since the operation mode can be automatically switched based on the comfort detection calculation based on the comfort detection calculation, energy saving can be achieved without unnecessary cooling and heating, and the effect of comfortable cooling and heating can be obtained.

The operation control method according to the present invention has been described above, and then the characteristic apparatus of the absorption cogeneration system according to the present invention will be described. 5 and 6 show FIG.
6 shows a configuration example of the auxiliary solution heating means 99 and the high temperature regenerator 1, and FIG. 6 is a view mainly showing the auxiliary solution heating means 99 from the right side of FIG. One end of the auxiliary solution heating means 99 is connected to a dilute solution conduit 42 via a float valve which is one of the solution circulation amount control means 14 in the float box 34 arranged at the solution outlet of the high temperature regenerator 1. The other end is connected to a further side of the eliminator 30a disposed before the steam conduit 41 of the high-temperature regenerator 1. The dilute solution passed through the high-temperature heat exchanger 7 is supplied to the float valve 14
And flows into the gas-liquid heat exchanger 101 from the bottom of the auxiliary solution heating means 99. Here, the exhaust gas 98 is controlled by the exhaust gas flow rate control means 100 and is supplied from the exhaust gas inlet header 103 to the plurality of upper gas passages 201a.
After flowing through the lower gas passages 201b via the exhaust gas reversing duct 109 and heating the dilute solution flowing through the solution passage 202, the exhaust gas exhaust duct 108 passes through the exhaust gas outlet header 104. Leaked to Here, between the gas passages 201a or between the gas passages 20a.
A solution passage 202 is disposed between the gas passages 1b, and a wall of each gas passage serves as a heat transfer wall to exchange heat between the solution and the exhaust gas. In particular, heat transfer fins are arranged on the heat transfer walls of the gas passages, and turbulence promoters are arranged to improve the heat transfer performance. A drain vent 105 is disposed below the exhaust gas outlet header 104. This is because when the temperature of the heat transfer wall at the start of operation is still at 80 ° C. or below and at a temperature level at which moisture in the exhaust gas 98 condenses, the drain 105 is appropriately opened to discharge condensed water, and the gas passage is condensed. It is provided in order to prevent blockage. Further, since the pH of the condensed water is extremely low, if the condensed water is retained for a long time without being discharged, corrosion and deterioration of the constituent devices will proceed. For this purpose, drainage is indispensable.

5 and 6, the cross-sectional area of the upper gas passage 201a is changed to the lower gas passage 201b.
Is wider than the gas flow path cross-sectional area. Accordingly, the gas flow velocity in the upper gas passage 201a through which the high-temperature exhaust gas flows becomes slower, and the heat transfer coefficient on the gas side decreases, so that the temperature rise on the heat transfer surface can be suppressed. On the other hand, in the lower gas passage 201b, since the exhaust gas temperature is lowered by heat exchange, the heat transfer rate on the gas side is increased with a faster gas flow rate, and the size is reduced. This makes it possible to provide the gas-liquid heat exchanger 101 having corrosion resistance and being small and lightweight.

Further, in this configuration, the dilute solution is first heated and boiled by passing through the auxiliary solution heating means 99, and the solution conduit 106 is heated.
And then introduced into the high-temperature regenerator 1. According to this configuration, since the boiling point is lower when the solution concentration is low even at the same pressure, there is an advantage that the heat exchange temperature difference between the auxiliary solution heating means 99 and the exhaust gas 98 can be made large. Accordingly, the gas-liquid heat exchanger 101 can be reduced in size and weight, or the effect of lowering the temperature of the exhaust gas discharged from the gas-liquid heat exchanger 101 to increase the efficiency of exhaust gas heat recovery and utilization can be obtained.

FIG. 7 shows an example in which the installation position of the auxiliary solution heating means 99 in FIG. 2 is changed. First, the dilute solution is supplied to the high temperature regenerator 1 and then the auxiliary solution heating means 99 is supplied. That the high-temperature regenerator 1 has a combustion chamber 29 at the lower part thereof, and a group of heat transfer tubes 102 disposed thereon to exhaust combustion gas from the burner 25 side; That the float box 34, which is a hole, is disposed in the auxiliary solution heating means 99, the eliminator 30a,
Placing the vapor conduit 41 in the auxiliary solution heating means 99;
The fact that only one of the passages 201 is provided for the exhaust gas of the gas-liquid heat exchanger 101 and that the liquid depth of the gas-liquid heat exchanger 101 is made shallow are the same as those of FIGS. This is the difference.

According to the configuration shown in FIG. 7, when the amount of heat recovered from the exhaust gas is large, the eliminator 30a is disposed closer to the auxiliary solution heating means 99 that generates a large amount of steam. . Further, since the heat exchange between the concentrated solution of the intermediate concentration and the exhaust gas 98 causes the boiling point to increase, the solution liquid depth of the gas liquid heat exchanger 101 can be reduced by the amount corresponding to the decrease in the heat exchange temperature difference. The effect that steam is easily generated is obtained. Further, since it is not necessary to divide the exhaust gas passage into upper and lower parts, the exhaust gas reversal duct 109 of the heat exchanger is not required, and since there is no need for a return exhaust gas passage, there is an effect that it can be manufactured at low cost. . Needless to say, the gas heat exchanger 101 may have a structure in which upper and lower gas passages are provided as in FIGS.

As another method of installing the auxiliary solution heating means, although not shown, the dilute solution having passed through the high-temperature heat exchanger 7 of FIG.
Alternatively, it is also possible to adopt a configuration in which the other is supplied to the auxiliary solution heating means, heat-concentrated in each case, the heat-concentrated solutions are combined, and then sent to the low-temperature regenerator 2.

[0047]

According to the present invention, the fuel consumption of the absorption chiller / heater can be significantly reduced by effectively utilizing the exhaust gas of the power generation engine and the exhaust heat via the jacket cooling water. In addition, by giving priority to the exhaust gas and subsequently the fuel, there is an effect that a quick and comfortable air conditioning operation can be performed. Further, by using the operation control method and the exhaust gas heat exchanger according to the present invention, a safer, smaller, and more efficient absorption chiller / heater can be realized.

[Brief description of the drawings]

FIG. 1 is a system diagram showing a configuration example of an absorption type cogeneration system according to the present invention.

FIG. 2 is a diagram showing a configuration example of an exhaust heat utilization absorption chiller / heater in the system of FIG. 1;

FIG. 3 is a flowchart showing an example of an operation control method of the absorption chiller / heater characterized by the present invention.

FIG. 4 is a flowchart showing another example of the operation control method of the absorption chiller / heater characterized by the present invention.

FIG. 5 is a diagram showing a configuration example of an auxiliary solution heating means according to the present invention.

6 is a view of the device of FIG. 5 from another angle.

FIG. 7 is a diagram showing another configuration example of the auxiliary solution heating means according to the present invention.

FIG. 8 is a diagram showing an actual measurement example of a high-temperature water heating amount and an exhaust gas heating amount with respect to an engine input.

[Explanation of symbols]

 DESCRIPTION OF SYMBOLS 1 High temperature regenerator 2 Low temperature regenerator 3 Condenser 4 Evaporator 5 Absorber 6 Low temperature heat exchanger 7 High temperature heat exchanger 8 Solution circulation pump 25 Burner 26 Fuel control means 32 Control panel 60 Engine 61 Generator 68 High temperature water heat exchange Device 70 Solution heating means 71 High-temperature water introduction conduit 72 High-temperature water circulation means 76 Temperature sensor 77 High-temperature water circulation amount control means 78 High-temperature water 80 Power generation module 81 Absorption chiller / heater 82 Exhaust heat absorption chiller / heater 83 Cooling / heating water 86 Cooling water 98 Gas 99 auxiliary solution heating means 100 exhaust gas flow rate control means 101 gas liquid heat exchanger 115 pressure sensor 116 temperature sensor 201a upper gas passage 201b lower gas passage 202 solution passage

 ──────────────────────────────────────────────────の Continuing on the front page (72) Inventor Satoru Endo 603, Kandamachi, Tsuchiura-shi, Ibaraki Pref. Inside the Tsuchiura Plant, Hitachi, Ltd. Inside the Tsuchiura Plant (72) Inventor Masahiro Oka 4-20-8-405 Uesinozaki, Edogawa-ku, Tokyo (72) Inventor Yukimaro Murata 2-45-12-405 Fujimidai, Kunitachi-shi, Tokyo

Claims (20)

[Claims] 1. An absorption chiller / heater having at least a high-temperature regenerator, a low-temperature regenerator, a condenser, an evaporator, an absorber, a low-temperature heat exchanger, and a high-temperature heat exchanger as components thereof, and a generator driving engine. Solution heating means for performing heat exchange between high-temperature water generated by jacket cooling and a solution of a cycle flowing in the absorption chiller / heater; and high-temperature water circulating means for circulating the high-temperature water to the solution heating means. Auxiliary solution heating means for performing heat exchange between exhaust gas of the engine and a solution of a cycle flowing in the absorption chiller / heater, and an exhaust gas for flowing the exhaust gas through the auxiliary solution heating means Introduction means; fuel control means for controlling the amount of fuel supplied to a burner provided in the high-temperature regenerator; and high-pressure control means for controlling the amount of high-temperature water circulated to the solution heating means. An exhaust cogeneration system utilizing exhaust heat of an engine, comprising: hot water circulation amount control means; and exhaust gas flow rate control means for controlling the flow rate of exhaust gas flowing through the auxiliary solution heating means. 2. The absorption cogeneration system utilizing exhaust heat of an engine according to claim 1, wherein the auxiliary solution heating means is provided between the high temperature water and a dilute solution from the high temperature heat exchanger to the high temperature regenerator. An absorption cogeneration system utilizing engine exhaust heat, wherein the cogeneration system is arranged to perform heat exchange. 3. The absorption cogeneration system utilizing exhaust heat of an engine according to claim 1, wherein the dilute solution flowing out of the high-temperature heat exchanger of the absorption chiller / heater is used for two times.
An absorption-type cogeneration system utilizing exhaust heat of an engine, wherein one of the components is heated and concentrated by a high-temperature regenerator, and the other is heated and concentrated by the auxiliary solution heating means. 4. The cogeneration system according to claim 1, wherein the auxiliary solution heating means exchanges heat between the solution concentrated in the high temperature regenerator and the high temperature water. An absorption-type cogeneration system utilizing engine exhaust heat, wherein the cogeneration system is arranged to perform. 5. The operation control method for an absorption cogeneration system utilizing exhaust heat of an engine according to claim 1, wherein said first calculation means calculates a required cooling / heating capacity required for said absorption chiller / heater. Second computing means for calculating the amount of high-temperature water heat that can be taken into the solution cycle of the absorption chiller / heater from the high-temperature water by the solution heating means; and A third calculating means for calculating the amount of exhaust gas heat that can be taken into the solution cycle; and the exhaust gas as a heat source for realizing the required cooling and heating capacity calculated by the first calculating means; Priorities for using the high-temperature water and the burner are determined in advance, and the relationship between the required cooling and heating capacity, the high-temperature water heating amount, and the magnitude of the exhaust gas heating amount and An operation control method, wherein the operation control of the fuel control means, the high-temperature water circulation amount control means, and the exhaust gas flow rate control means is performed based on the priority. 6. The operation control method according to claim 5, wherein the first calculating means determines a required cooling and heating capacity from the inlet and outlet temperatures of the cold and hot water of the absorption chiller and hot water and the flow rate of the cold and hot water. Calculating, further comparing the calculated required cooling / heating capacity with the maximum heat input limit set for the heat cycle of the absorption chiller / heater, and outputting a smaller value as the required cooling / heating capacity. Characteristic operation control method. 7. The operation control method according to claim 5, wherein the second calculating means includes an inlet temperature of the high-temperature water to the solution heating means, an inlet temperature of the solution, and the solution heating means of the high-temperature water. A first table having a content of a high-temperature water heat amount determined in advance by measurement for a plurality of values of a circulation amount to the hot water supply port. When the first condition that the temperature is higher than the temperature is satisfied, the maximum circulation amount of the high-temperature water that can be circulated to the solution heating means, which is determined according to the operation state of the engine, and the detected high temperature The value of the high-temperature water heat quantity corresponding to the water inlet temperature and the solution inlet temperature is read out from the first table and set as an output value. When the first condition is not satisfied, the output is set to 0.
An operation control method characterized by: 8. The operation control method according to claim 5, wherein the second calculating means calculates a high-temperature water heat amount predetermined by measurement for a plurality of values of input or output to the engine. A first table having contents therein, and when a first condition that an inlet temperature of the high-temperature water detected at each time point is higher than an inlet temperature of the solution is satisfied, a detected input or output of the engine. Is read from the first table as an output value, and when the first condition is not satisfied, the output is set to 0.
An operation control method characterized by: 9. The operation control method according to claim 5, wherein the third calculation means includes an exhaust gas inlet temperature and a solution inlet temperature to the auxiliary solution heating means, and the auxiliary solution of the exhaust gas. A second table containing exhaust gas heat amounts determined in advance by measurement for a plurality of values of the flow rate to the heating means, wherein the inlet temperature of the exhaust gas detected at each time point is the solution When the second condition that is higher than the inlet temperature of the engine is satisfied, the maximum flow rate of the exhaust gas that can flow through the auxiliary solution heating means, which is determined according to the operating state of the engine, The exhaust gas heating value corresponding to the detected exhaust gas inlet temperature and solution inlet temperature is read from the second table and used as its output value, and the second condition is not satisfied. When, the output 0
An operation control method characterized by: 10. The operation control method according to claim 5, wherein the third calculating means calculates an exhaust gas heat amount predetermined by measurement for a plurality of values of input or output to the engine. A second table having contents, wherein when the second condition that the exhaust gas inlet temperature detected at each time point is higher than the solution inlet temperature is satisfied, the detected engine input or output Is read from the second table as an output value, and when the second condition is not satisfied, the output is set to 0.
An operation control method characterized by: 11. The operation control method according to claim 5, wherein the operation control for at least one of the high-temperature water circulation amount control means and the exhaust gas flow rate control means includes an OFF state in which the flow rate is set to 0. An operation control method, which is an on-off control for setting any one of the maximum on-states. 12. The operation control method according to claim 5, wherein the operation control for at least one of the high-temperature water circulation amount control means and the exhaust gas flow rate control means is a control for continuously changing the flow rate. An operation control method, characterized in that: 13. The operation control method according to claim 5, wherein, when a request for heat input to the burner becomes equal to or less than a minimum combustion capacity possible with the burner, combustion of the burner is stopped. Operation control method. 14. The operation control method according to claim 5, wherein when a demand for heat input to the burner is less than a minimum combustion capacity possible with the burner, the burner is always burned at the minimum combustion capacity. An operation control method characterized by the above-mentioned. 15. The operation control method according to claim 5, wherein the first of the priorities of the heat sources to be used is exhaust gas, and when the heat use of exhaust gas alone is insufficient, high-temperature water is supplied to the second.
An operation control method characterized by utilizing the combustion of a burner as a third heat source when the heat source is used as a third heat source. 16. The operation control method according to claim 5, wherein the first priority of the heat source to be used is exhaust gas, and combustion of the burner is performed by the second heat source when heat utilization of exhaust gas alone is insufficient. An operation control method, wherein high-temperature water is used as a third heat source when there is a shortage. 17. The operation control method according to claim 7, wherein the high-temperature water is not circulated to the solution heating unit when the high-temperature water heating amount calculated by the second calculation unit is 0. An operation control method characterized by the following. 18. The operation control method according to claim 9, wherein the exhaust gas does not flow through the auxiliary solution heating means when the exhaust gas heating value calculated by the third calculation means is zero. An operation control method characterized by the above-mentioned. 19. The operation control method according to claim 6, wherein the limit value of the maximum heat input is set higher than the value when the solution temperature of the high-temperature regenerator is in a predetermined temperature range. The operation control, wherein the value when the cooling water temperature of the absorption chiller / heater is lower than a value when the cooling water temperature of the absorption chiller / heater is equal to or higher than a predetermined threshold is set to be smaller when the temperature is not within the range. Method. 20. The operation control method according to claim 5, wherein the solution circulation amount is variably controlled according to the operation condition of the absorption chiller / heater at that time.