KR20130010470A - Method for generating power from exhaust heat and system for generating power from exhaust heat - Google Patents

Abstract

It is a heat generation method using the heat source discharged from an incinerator effectively. This heat generation method is a separator in which hot air 2 heated by the exhaust gas from the incinerator 101 included in the sewage treatment system S is upstream than the turbine 10 in the power generation system G. The heater 17 which is applied to the superheater 19 which is downstream from (18), and performs heat exchange with the working fluid L, and the hot air 2 after that, is upstream than the separator 18, And a second heat exchange step of performing heat exchange with the working fluid L, and washing the exhaust gas and washing the exhaust gas from the sewage treatment system S and the hot air 2 after the heater 17. A third heat exchange step of performing heat exchange with the working fluid L by applying a heat exchange step for drainage to perform heat exchange, and subsequent thin water drainage W to the evaporator 16 upstream from the heater 17; (2) has a contacting step of contacting the exhaust gas.

Description

METHOD FOR GENERATING POWER FROM EXHAUST HEAT AND SYSTEM FOR GENERATING POWER FROM EXHAUST HEAT

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a heat generation power generation method and a heat generation power generation system, and more particularly, to a heat generation power generation method and a heat generation power generation system using heat of high temperature exhaust gas discharged from an incinerator such as a sewage sludge incinerator or a waste incinerator.

In recent years, measures against global warming and environmental issues have been important, and expectations for energy-saving technologies are increasing year by year. As a countermeasure against such environmental problems, the effective use of new energy and unused energy has attracted attention, and for example, attempts have been made to calculate new energy using energy that has been discarded without being effectively used.

For example, Patent Literature 1 discloses a configuration in which steam is generated using the heat of retention of exhaust gas generated from a sewage sludge incinerator, and power generation is performed by the steam. In addition, Patent Literature 2 discloses a configuration in which power is generated by superheating steam by using combustion gas generated by waste incineration and inducing the steam to a steam turbine. In addition, Patent Literature 3 discloses a configuration in which the working liquefaction medium of the power generation system is evaporated by the retention heat of the sewage wastewater obtained from the flue gas treatment system of the sewage treatment system, and the turbine is driven by the working medium steam to generate power. have.

In this way, when incineration of waste or sludge occurs, hot gas and waste water are generated. However, there are many proposals for recovering a part of the waste energy in the form of electric energy by using these thermal energy, which has been disposed in the past, for power generation.

Taking the sewage sludge incinerator as an example, the temperature of the exhaust gas from the incinerator is about 800 ° C to 850 ° C. In a typical incineration plant, a high temperature exhaust gas from the incinerator is passed through a smoke prevention air preheater or other heat exchanger to recover a part of the array, and then dust is removed from the dust collector and passed through the flue gas scrubber. It is made to wash with water, and components, such as NOX and SOX, in exhaust gas are removed.

When the incinerator is a flow incinerator, a flow air preheater may be provided at the front end of the smoke prevention air preheater. In the case where the collector is a ceramic filter, high temperature dust collection is possible. In the case of a bug filter, dust collection is performed after the temperature is lowered to 300 ° C or lower in a cooling tower.

In the exhaust gas treatment system of such a normal incineration plant, the exhaust gas of 200 degreeC-400 degreeC is cooled to about 40 degreeC by the flue gas scrubber tower, and the sewage wastewater is discharged about 60 degreeC-70 degreeC. Although this sediment drainage is relatively low temperature, since the specific heat of water is large, a large amount of heat is large and it exceeds 50% of the amount of heat which a discharge gas has.

Patent Document 1: Japanese Patent Publication No. 2005-321131 Patent Document 2: Japanese Patent Application Laid-Open No. 9-310606 Patent Document 3: Japanese Patent Application Laid-Open No. 9-32513

However, what was described in each of said patent documents 1-3 only applies the heat source discharged | emitted at the time of incineration of waste etc. to a power generation system, and it cannot be said that the efficiency of energy utilization is high enough. The recovery efficiency of thermal energy varies greatly depending on the position and application method of applying the heat source to the power generation system, but each of the above patent documents does not provide a sufficient proposal for improving the efficiency of such energy recovery.

In addition, the heat source discharged from the incinerator is not always constant, and the amount of heat may change. In such a case, if the discharge heat source is applied to the power generation system as it is, there is a problem that the power generation efficiency is affected by the change in the heat quantity of the discharge heat source, so that stable and efficient power generation cannot be performed.

SUMMARY OF THE INVENTION The present invention has been made in view of the above circumstances, and it is an object of the present invention to provide an array generation method and an array generation system that can efficiently use a heat source discharged from an incinerator, improve its energy recovery efficiency, and generate electricity stably and efficiently. It is an exemplary subject.

In order to solve the above problems, the heat generation method as an exemplary aspect of the present invention is to generate power by rotating a turbine with a working fluid for hot air heated by exhaust gas discharged from an incinerator of an incineration treatment system. A first heat exchange step of performing heat exchange between the hot air and the working fluid at the first position by applying the first position upstream than the turbine and downstream from the separator on the working fluid path in the array power generation system, and the first position The second heat exchange step of performing heat exchange between the hot air at the second position and the working fluid by applying the hot air after the heat exchange at the second position to an upstream side of the separator on the working fluid path, and cleaning the exhaust gas. The wastewater discharged from the incineration treatment system afterwards and the heat exchanger performing the heat exchange of the hot air after heat exchange at a 2nd position. A third heat exchange step for performing heat exchange between the sewage drainage at the third position and the working fluid by applying the heat exchange step for heat exchange and the duct drainage after the heat exchange with the hot air to a third position upstream of the second position on the working fluid path. A heat exchange step and a contact step of bringing the hot air after heat exchange with the sewage drainage into contact with the exhaust gas as white smoke prevention air.

Since hot air from the incineration treatment system is applied to the heat generating system, heat exchange is performed between the hot air and the working fluid, so that efficient power generation can be performed using waste heat. In addition, since the high-temperature air is applied to the heat generating system in a plurality of places at the first position upstream of the turbine and downstream of the separator and the second position upstream of the separator, the amount of heat exchange with the working fluid is increased. It can be enlarged and sufficient heat can be given to a working fluid.

Heat exchange is first performed at a first position after the separator in which the working fluid is in the gaseous state, thereby overheating the working fluid in the gaseous state. Thereafter, the working fluid is heat-exchanged at the second position before the separator in the gas-liquid two-phase state to promote vaporization of the working fluid. The hot air imparts excess heat to the working fluid in a gas-liquid two-phase state having a large heat capacity after applying heat to the working fluid in a gas state having a low heat capacity. Therefore, efficient heat exchange can be performed, and further, it can contribute to suppression of the fall of power generation efficiency, and suppression of the fall of power generation amount.

After the heat exchange at the second position, heat exchange between the hot air and the sediment drainage is performed, and heat exchange between the sediment waste water and the working fluid after heat exchange with the hot air is performed at a third position upstream from the second position. Therefore, the waste heat discharged from the incineration treatment system in the form of hot air or sewage drainage can be sufficiently reused and used for heat generation.

In a general example, the temperature of the hot air heated by the exhaust gas in the incineration treatment system is about 300 ° C, and the temperature of the hot air after heat exchange at the first position is about 170 ° C to 200 ° C. In addition, the temperature of the hot air after heat exchange in a 2nd position is about 100 to 150 degreeC. Moreover, the temperature of the duct waste water from an incineration treatment system is about 60 to 70 degreeC, and the temperature of the duct waste water after heat exchange with hot air is about 70 degreeC-73 degreeC.

The temperature of the hot air after heat exchange with the duct waste water is still at a high temperature of about 90 ° C. to 100 ° C., and the hot air can be sufficiently used as the anti-smoke smoke if it is brought into contact with the exhaust gas from the incinerator. Therefore, in this heat generating power generation method, a large amount of heat exchange is performed until high temperature air is used as the white smoke prevention air without impairing the function as the white smoke prevention air, thereby achieving efficient energy recovery.

Since the sewage drainage after heat exchange with hot air rises to a temperature of about 70 ° C to 73 ° C, by applying the sewage drainage to the third position and performing heat exchange with the working fluid, energy recovery can be further improved. Can be.

Condensing each hot air from the plurality of incineration treatment systems over the plurality of incineration treatment systems before the heat exchange at the first position, and each fine wastewater from the plurality of incineration treatment systems before the heat exchange with the hot air. It may further have a step of aggregation throughout the incineration treatment system.

The situation of waste disposal such as sewage sludge and garbage in one incineration processing system is not constant. Therefore, the discharge | emission, temperature (calorie | heat amount), etc. of hot air from one incineration processing system, and sewage wastewater cannot be said to be stable.

However, by collecting each hot air or sewage wastewater from a plurality of incineration treatment systems, and then applying the same to an in-line power generation system, energy recovery can be stabilized, and the advantages of the scale of the in-line power generation system can be utilized.

For example, in an incineration processing system having a large incineration capacity (for example, 5 units of a normal capacity), there is a limit of enlargement or there is a risk that the incineration processing system stops at regular maintenance or failure. Therefore, when five capacity | capacitances are needed, it does not make a large incineration processing system but connects and uses five normal incineration processing systems.

At this time, when five incineration power generation systems having five normal capacities are connected to each other, the installation cost of the five thermal power generation systems is required and the cost is high. In addition, when the incineration treatment system is operated, each heat generating power system normally operates as close to the maximum capacity as possible, so that the metal temperature of the heat exchanger at the first position rises to the limit (the temperature difference is small and heat exchange is not performed very much. ), Which is undesirable in view of device life.

However, when intensively connecting a large-scale (e.g., 5 units of normal capacity) heat generation system to 5 incineration processing systems of normal capacity, firstly, the equipment cost of the heat generation power generation system is only 1 unit. There is an advantage. In addition, if five incineration systems are not in operation at all, and an average of three incineration systems are in operation, the capacity of the heat exchanger at the first position of the large array power generation system ( We can do with capacity for three) without making large. Therefore, there is also a cost advantage of the heat exchanger in that respect.

Moreover, when the heat generating power generation system itself is large in size and has a space in capacity, and when the metal temperature of the heat exchanger in a 1st position does not rise so much, it can contribute to the improvement of the lifetime of a heat exchanger. Here, "aggregation across a plurality of incineration treatment systems" is not limited to the case where there are a plurality of incineration treatment systems as a whole and aggregates them, and "a plurality of incinerators exist in the incineration treatment system, and in these incinerators" Over aggregate ”. In the following text, the same applies to the case where "aggregation across a plurality of incineration treatment systems" includes the case where "a plurality of incinerators exist in an incineration treatment system and are aggregated across these incinerators".

In the aggregation of each hot air, adjustment means (adjustment valves, etc.) which adjust the discharge | emission from each incineration processing system may be provided in a discharge path, and these adjustment means may of course be adjusted by computer control, and each incineration process The same is true for the sewage drainage from the system.

A first heat exchange avoidance step of joining the hot air with the hot air after the heat exchange at the first position without applying the hot air to the first position, and after the heat exchange at the second position without applying the hot air after the joining to the second position You may further have a second heat exchange avoidance step of joining hot air.

Heat exchange at the first position or the second position of the hot air and the working fluid can be avoided as necessary. Therefore, the heat exchange between the hot air and the working fluid can be performed or stopped in accordance with the hot air from the incineration treatment system, the discharge and temperature (heat quantity) of the sewage drainage, or the amount of power required by the heat generating system. .

In addition, heat exchange is performed only in the first position and heat exchange is avoided in the second position, heat exchange is avoided only in the first position, and heat exchange is performed in the second position, or heat exchange is performed in both the first position and the second position. In this case, the heat exchange execution position can be selected according to the situation.

For example, the heat transfer area of the heat exchanger in the first position is relatively large and the heat transfer area of the heat exchanger in the second position is relatively small, whereby the heat exchange efficiency in the first position is higher than the heat exchange efficiency in the second position. In this case, when all the hot air is applied to the first position, heat exchange may be performed more than necessary.

However, if the heat exchange between the hot air and the working fluid at the first position can be avoided by the first heat exchange avoiding step, an appropriate heat recovery in accordance with the power generation necessary amount can be performed. Therefore, for example, a so-called backlash etc. can be prevented by generating excessive generated electric power beyond the required electric power on the load side (electric power consumption side).

Of course, if not only whether to avoid the heat exchange between the hot air and the working fluid in the first position or the second position, but also the amount of avoidance can be adjusted, an appropriate amount of power generation can be further performed as necessary. For example, in addition to the first and second heat exchange avoidance steps, by having a first and second adjustment steps (for example, a flow rate adjustment step by a flow rate adjustment valve or the like) to be described later, the amount and the amount of hot air applied to each heat exchange position are avoided. If it can be adjusted, it is possible to finely adjust the heat exchange amount (that is, the application amount of the hot gas) in accordance with the required power generation amount.

The adjustment effect of the generation amount (generation power) by adjusting the application amount / avoidance amount of hot air is high when the heat transfer area of the heat exchanger in a 1st position is large, and its effect is low when the heat transfer area is small. In other words, when the heat transfer area of the heat exchanger in the first position is small, there is little decrease in power generation amount when the application amount of hot air is reduced (increased the evacuation amount), and the fluctuation of the heat output side when there are a plurality of incinerators is considered. The investment effect is also high.

By using this property, if the heat transfer area of the heat exchanger of either the first position or the second position is set larger and the other is set smaller, the amount of hot air applied to the heat exchanger having the larger heat transfer area and the avoidance amount are adjusted. By doing so, it is possible to precisely and effectively adjust the amount of power generation as required. This is because, in the heat exchanger having the smaller heat transfer area, even if the amount of heat input by hot air fluctuates somewhat, the influence on the power generation amount is small.

In addition, when the heat transfer area of the heat exchanger in the first position is small, since the degree of change in the amount of power generated by the change in the amount of applied hot air is small, it is possible to secure a stable amount of power generated even if the amount of hot air changes. For example, in the case where hot air from a plurality of incineration systems is collected and used in a heat generating system, not all the incineration systems are always in operation, and some incineration systems may be inoperative.

Even in such a case, if the heat transfer area of the heat exchanger at the first position is set relatively small, even if the amount of hot air decreases due to some non-operation, the decrease in the amount of generated power can be suppressed as much as possible. By setting the heat transfer area of the heat exchanger small, the cost of the heat exchanger can also be reduced.

Measuring a first working fluid temperature of the working fluid after the heat exchange at the first position, measuring a first hot air temperature of the hot air before the heat exchange at the first position, the first hot air temperature and the first A first adjustment step of adjusting the distribution of the amount of hot air to be applied to the first position and the amount of hot air to avoid application to the first position based on the difference of the working fluid temperature, and of the working fluid after heat exchange at the second position. Measuring a second working fluid temperature, measuring a second hot air temperature of the hot air before heat exchange at the second position, and based on a difference between the second hot air temperature and the second working fluid temperature You may further have a 2nd adjustment step which adjusts distribution of the amount of hot air applied to a position, and the amount of hot air which avoids application to a 2nd position.

Based on the temperature difference between the first working fluid temperature and the first hot air temperature, an appropriate heat exchange based on the temperature difference at the first position can be realized because the hot air amount distribution to be applied / not applied to the first position is adjusted. For example, when this temperature difference is small, heat exchange is not performed very much even if hot air is applied to the first position. In such a case, it is preferable to reduce the amount of hot air applied to the first position and to increase the amount of hot air that avoids (does not apply) the first position.

In addition, since the hot air amount distribution to be applied / not applied to the second position is adjusted based on the temperature difference between the second working fluid temperature and the second hot air temperature, appropriate heat exchange based on the temperature difference can be realized even at the second position. have. For example, when this temperature difference is small, heat exchange is not performed very much even if hot air is applied to the second position. In such a case, it is preferable to reduce the amount of hot air applied to the second position and to increase the amount of hot air that avoids (does not apply) the second position.

Measuring a first working fluid temperature of the working fluid immediately before the heat exchange at the first position, measuring a first hot air temperature of the hot air before the heat exchange at the first position, the first hot air temperature and the first temperature A first adjustment step of adjusting the distribution of the amount of hot air to be applied to the first position and the amount of hot air to avoid application to the first position based on the difference of 1 working fluid temperature, and the operation immediately before the heat exchange at the second position Measuring a second working fluid temperature of the fluid, measuring a second hot air temperature of the hot air before heat exchange at the second position, and based on a difference between the second hot air temperature and the second working fluid temperature Of course, you may have a 2nd adjustment step which adjusts distribution of the amount of hot air applied to a 2nd position, and the amount of hot air which avoids application to a 2nd position.

The heat generation method as another exemplary aspect of the present invention comprises the steps of: aggregating each hot air heated by exhaust gas respectively discharged from a plurality of incinerators provided in a plurality of incineration treatment systems over a plurality of incineration treatment systems; By applying the concentrated hot air to the first position upstream from the turbine in the working fluid path in the heat generating system in which the turbine generates power by rotating the turbine by the working fluid, the hot air at the first position And a first heat exchange step for performing heat exchange, and a contact step for bringing the hot air after the heat exchange at the first position into the exhaust gas as contact with the exhaust gas.

Since hot air from the incineration treatment system is applied to the heat generating system, heat exchange is performed between the hot air and the working fluid, so that efficient power generation can be performed using waste heat. But the situation of waste disposal such as sewage sludge and garbage in one incineration treatment system is not constant. Therefore, the discharge | emission, temperature (calorie | heat amount), etc. of hot air from one incineration processing system, and sewage wastewater cannot be said to be stable.

However, by condensing each hot air from a plurality of incineration treatment systems, and then applying the same to an in-line power generation system, energy recovery can be stabilized as described above, and the advantages of the scale of the in-line power generation system can be utilized. . For example, by condensing hot air from a plurality of incineration treatment systems and sewage wastewater, and applying them to one large array power generation system, the apparatus cost can be reduced as compared with installing a plurality of array power generation systems. Moreover, it can also contribute to the lifetime improvement of an array power generation system.

In the aggregation of each hot air, adjustment means (adjustment valve etc.) which adjust the discharge | emission from each incineration treatment system may be provided in the discharge path | route, and these adjustment means may be adjusted by computer control of course.

The temperature of the hot air after heat exchange with the working fluid is generally still sufficiently hot, and when the hot air comes into contact with the exhaust gas from the incinerator, it can be sufficiently used as anti-smoke smoke. Therefore, in this heat generating power generation method, heat exchange with the working fluid is carried out until high temperature air is used as the white smoke prevention air without impairing the function as the white smoke prevention air, thereby achieving efficient energy recovery.

When the first position is downstream of the separator in the heat generating system, the second position by applying hot air after the first heat exchange step and before the contacting step to a second position upstream of the separator on the working fluid path. It may further have a second heat exchange step of performing heat exchange of the working fluid with the hot air in the furnace.

Heat exchange is first performed at a first position after the separator in which the working fluid is in the gaseous state, thereby overheating the working fluid in the gaseous state. Thereafter, the working fluid is heat-exchanged at the second position before the separator in the gas-liquid two-phase state to promote vaporization of the working fluid. The hot air imparts excess heat to the working fluid in a gas-liquid two-phase state having a large heat capacity after applying heat to the working fluid in a gas state having a low heat capacity. Therefore, efficient heat exchange can be performed, and further, it can contribute to suppression of the fall of power generation efficiency, and suppression of the fall of power generation amount.

In order to cool the working fluid after the turbine is rotated, applying the coolant to a position downstream from the turbine in the working fluid path, and contacting the coolant after the working fluid cooling with the exhaust gas as fine water; You may have it.

Since the cooling water of the working fluid is brought into contact with the discharged gas as fine water, it can contribute to saving of the quantity used throughout the incineration treatment system and the heat generating power system. In addition, since the cooling water is heated up after cooling the working fluid (that is, heat exchange with the working fluid), when the cooling water is used for water supply to the flue gas scrubbing tower of the incineration treatment system, the cooling water contributes to an increase in the tower temperature, and thus the temperature of the sewage drainage is increased. The height is effective.

The working fluid may be any of ammonia, prolon or ammonia / water mixed fluid.

These fluids tend to vaporize at relatively low temperatures. Therefore, by using these fluids as working fluids, heat generation using a temperature difference can be realized by effectively utilizing heat from waste heat (low temperature heat source), which has a low temperature but is present in large quantities.

An array power generation system as still another exemplary aspect of the present invention is an array power generation system that generates power by rotating a turbine by a working fluid, and includes hot air heated by exhaust gas discharged from an incinerator included in an incineration treatment system. A first heat exchange function for performing heat exchange between the hot air at the first position and the working fluid at the first position by applying to a first position upstream than the turbine on the working fluid path and downstream from the separator, and the high temperature after heat exchange at the first position. By applying air to a second position upstream than the separator on the working fluid path, the second heat exchange function performs heat exchange between the hot air and the working fluid at the second position, and from the incineration treatment system after cleaning the exhaust gas. A heat exchange function for drainage for performing heat exchange between the discharged duct drainage and the hot air after the heat exchange at the second position; A third heat exchange function for performing heat exchange between the sewage drainage at the third position and the working fluid by applying the sewage drainage after the heat exchange with the hot air to a third position upstream from the second position on the working fluid path; It has a contact function which makes high temperature air after heat exchange with waste water contact with exhaust gas as white smoke prevention air.

Since hot air from the incineration treatment system is applied to the heat generating system, heat exchange is performed between the hot air and the working fluid, so that efficient power generation can be performed using waste heat. In addition, since the high-temperature air is applied to the heat generating system in a plurality of places at the first position upstream of the turbine and downstream of the separator and the second position upstream of the separator, the amount of heat exchange with the working fluid is increased. It can be enlarged and sufficient heat can be given to a working fluid.

Heat exchange is first performed at a first position after the separator in which the working fluid is in the gaseous state, thereby overheating the working fluid in the gaseous state. Thereafter, the working fluid is heat-exchanged at the second position before the separator in the gas-liquid two-phase state to promote vaporization of the working fluid. The hot air imparts excess heat to the working fluid in a gas-liquid two-phase state having a large heat capacity after applying heat to the working fluid in a gas state having a low heat capacity. Therefore, efficient heat exchange can be performed, and further, it can contribute to suppression of the fall of power generation efficiency, and suppression of the fall of power generation amount.

Further, after the heat exchange at the second position, heat exchange between the hot air and the sewage drainage is performed, and heat exchange between the sediment waste water and the working fluid after heat exchange with the hot air is performed at a third position that is upstream from the second position. Therefore, the waste heat discharged from the incineration treatment system in the form of hot air or sewage drainage can be sufficiently reused and used for heat generation.

An array power generation system as still another exemplary aspect of the present invention is an array power generation system that generates power by rotating a turbine by a working fluid, and is heated by exhaust gases respectively discharged from a plurality of incinerators included in a plurality of incineration treatment systems. The hot air at the first position and the working fluid by applying the collected hot air over a plurality of incineration treatment systems, and applying the hot air after aggregation to a first position upstream of the turbine on the working fluid path. It has a 1st heat exchange function which heat-exchanges, and the contact function which makes high temperature air after heat exchange in a 1st position, and makes it come into contact with exhaust gas as a white smoke prevention air.

Since hot air from the incineration treatment system is applied to the heat generating system, heat exchange is performed between the hot air and the working fluid, so that efficient power generation can be performed using waste heat. But the situation of waste disposal such as sewage sludge and garbage in one incineration treatment system is not constant. Therefore, the discharge | emission, temperature (calorie | heat amount), etc. of hot air from one incineration processing system, and sewage wastewater cannot be said to be stable.

However, by condensing each hot air from a plurality of incineration treatment systems, and then applying the same to an in-line power generation system, energy recovery can be stabilized as described above, and the advantages of the scale of the in-line power generation system can be utilized. . For example, by condensing hot air from a plurality of incineration treatment systems and sewage wastewater, and applying them to one large array power generation system, the apparatus cost can be reduced as compared with installing a plurality of array power generation systems. Moreover, it can also contribute to the lifetime improvement of an array power generation system.

In the aggregation of each hot air, adjustment means (adjustment valve etc.) which adjust the discharge | emission from each incineration treatment system may be provided in the discharge path | route, and these adjustment means may be adjusted by computer control of course.

The temperature of the hot air after heat exchange with the working fluid is generally still sufficiently hot, and when the hot air comes into contact with the exhaust gas from the incinerator, it can be sufficiently used as anti-smoke smoke. Therefore, in this heat generating power generation method, efficient energy recovery is realized by performing heat exchange with the working fluid until the hot air is used as the smoke prevention air without impairing the function as the smoke prevention air.

Further objects or other features of the present invention will become apparent from the preferred embodiments described below with reference to the accompanying drawings.

According to the present invention, the heat source discharged from the incinerator can be effectively used, and the energy recovery efficiency can be improved to generate electricity stably and efficiently. For example, by applying hot air from an incineration treatment system equipped with the incinerator at a plurality of places in an array power generation system and using it as anti-smoke smoke, it is possible to realize efficient energy recovery of thermal energy that has been disposed of in the past and to fully achieve a smoke prevention function. Can be.

By integrating high-temperature air or fine wastewater from a plurality of incineration treatment systems and applying them to an in-line power generation system, the influence of changes in the operating conditions for each incineration treatment system is reduced, and stable energy recovery is realized. In addition, it is possible to adjust the amount of hot air applied to the tandem power generation system and the amount of hot air not to be applied, so that the amount of hot air applied to the tandem power generation system can be changed in response to the change in the amount of waste heat from the incineration treatment system and the required amount of power generation. Therefore, it is possible to stably generate the required amount appropriately.

BRIEF DESCRIPTION OF THE DRAWINGS It is a block diagram which shows schematic structure of the sewage treatment plant containing the power generation system which implements the heat generating power generation method which concerns on embodiment of this invention.
FIG. 2 is a block diagram illustrating an outline of an internal configuration of the processing system shown in FIG. 1.
3 is a block diagram illustrating an outline of an internal configuration of the power generation system shown in FIG. 1.
4 is a configuration diagram of a power generation system according to Embodiment 1 of the present invention.
5 is a configuration diagram of a power generation system according to Comparative Example 1 of the present invention.
6 is a configuration diagram of a power generation system according to Comparative Example 2 of the present invention.
7 is a configuration diagram of a power generation system according to Comparative Example 3 of the present invention.
8 is a configuration diagram of a power generation system according to Comparative Example 4 of the present invention.

EMBODIMENT OF THE INVENTION Hereinafter, the heat generating power generation system which implements the heat generating power generation method which concerns on embodiment of this invention is demonstrated using drawing. 1 is a block diagram showing a schematic configuration of a sewage treatment plant (hereinafter abbreviated as plant) P according to an embodiment of the present invention. The plant P is configured with a sewage treatment system (hereinafter abbreviated as treatment system) S and a power generation system (array power generation system) G as a plurality of incineration treatment systems. In this plant P, the high temperature air (white smoke prevention air) 2 from the processing system S, and the duct waste water W are applied to the power generation system G. In FIG. Each of the hot air 2 from each of the plurality of processing systems S and each of the sewage wastewaters W are concentrated and applied to the power generation system G, respectively.

In addition, the high-temperature air 2 after performing heat exchange in the power generation system G is the exhaust gas cleaning tower 105 of each treatment system S from the power generation system G as the anti-smoke smoke 2 (FIG. 2). To be sent). In addition, the cooling water C used for cooling the working fluid in the power generation system G is sent to the flue gas washing tower 105 of each treatment system S as a part of the thin water.

2 is a block diagram showing an outline of an internal configuration of the processing system S. As shown in FIG. Since the some processing system S has substantially the same structure, the structure of one processing system S is demonstrated and the description regarding the structure of another processing system S is abbreviate | omitted. This processing system S is roughly comprised with the incinerator 101, the fluidized air preheater 102, the smoke prevention air preheater 103, the dust collector 104, and the flue gas washing tower 105. As shown in FIG.

In FIG. 2, 101 is an incinerator, and in this embodiment, a fluid incinerator for incineration of sewage sludge dewatering cake. However, in the present invention, the incinerator 101 is not limited to this, but may be a waste incinerator. The exhaust gas is usually a high temperature exhaust gas of about 800 ° C to 850 ° C. 102 is a flow air preheater into which this hot exhaust gas is introduced, and preheats the flow air, for example, at 650 ° C., and supplies it to the distribution tube at the bottom of the furnace. If the incinerator 101 is not a flow incinerator, the flow air preheater 102 is omitted.

At the rear end of the flowing air preheater 102, a smoke prevention air preheater 103 is provided. This white smoke prevention air preheater 103 is a heat exchanger for obtaining the hot air (white smoke prevention air) 2 for preventing water vapor in the exhaust gas discharged from the chimney from appearing as white smoke, and a heating gas of about 300 ° C ( White smoke prevention air). On the other hand, when the exhaust gas passes through the smoke-preventing air preheater 103, the temperature is lowered to 250 ° C to 400 ° C, and is led to the next dust collector 104 to remove dust.

Here, as a typical example of the high temperature air (white smoke prevention air) 2, although air can be considered generally, various other gases may be applied. In addition, what heats by the smoke prevention air preheater 103, and is sent to the chimney 108 mentioned later is called hot air, and what sends it to the smokestack 108 and exhibits a smoke prevention function is called smoke smoke prevention air, Since both are substantially the same, the same reference numeral 2 is attached and demonstrated.

The dust collector 104 is a ceramic dust collector excellent in heat resistance in this embodiment, and can collect the discharge gas of 250 degreeC-400 degreeC which passed the white smoke prevention air preheater 103 as it is. However, as the dust collector 104, a bug filter may be used. In that case, it is necessary to arrange a cooling tower at the front end to lower the temperature to the heat resistance temperature of the bug filter. The temperature drop of the exhaust gas in the dust collector 104 is small, and the exhaust gas enters the next flue gas washing tower 105 at 200 ° C to 400 ° C.

The flue gas cleaning tower 105 removes components such as NOX and SOX in the exhaust gas by introducing exhaust gas from the lower portion of the tower and contacting water (fine water) W watered from the nozzle 106 in the upper portion. Device. As in the prior art, the water in the tower is pumped to the nozzle 106 by the pump 107 and used for circulation. In the flue gas washing tower 105 of this embodiment, the chimney 108 is connected to the upper part of the tower, and the exhaust gas cleaned in the tower is discharged from the chimney 108. The intermediate | middle part of the flue gas washing tower 105 and the chimney 108 is provided with the shelf board part 109 of several stages, and the water washing is studied so that sufficient water contact may be performed by fully contacting the clean water supplied from the upper part and discharge gas. .

In this flue gas washing tower 105, since the discharge gas contacts water, most of the heat of retention of the discharge gas of 200 degreeC-400 degreeC moves to the water side, and the thin waste water discharged | emitted from the flue gas washing tower 105 as mentioned above ( W) becomes hot water of 60 degreeC-70 degreeC. In the present invention, heat generation is performed using the heat of retention of the hot air 2 at about 300 ° C, but the heat of the sewage drainage W is also used.

For this reason, in this embodiment, after heat-retaining the fine smoke waste water W discharged | emitted from the flue gas washing tower 105 by heat exchange with the hot air 2 (drain heat exchange step, waste water heat exchange function), it arrange | positions, Supply to power generation system (G). The temperature increase range varies depending on the installation and the operation method, but is usually in the range of 5 ° C to 15 ° C. Since the hot air 2 after heat exchange with the duct waste water W maintains a temperature of about 90 ° C to 100 ° C, it is sent to the chimney 108 and can exhibit the original function as the smoke-free air 2.

In order to increase the temperature increase amount of the sewage drainage W, the temperature of the hot air 2 after heat exchange with the sewage drainage W (drainage heat exchange step, drainage heat exchange function) is lowered, but even if the temperature is lowered to about 100 ° C. In the climatic conditions of the air temperature of 20 ° C. and the humidity of 100%, white smoke does not form. However, white smoke occurs in the winter conditions of 0 ° C. and the humidity of 100%. However, there is no legal regulation on the occurrence of white smoke, and this condition is only a few days even in winter. In addition, the duct waste water W heated up by the heat exchange with the hot air 2 in this way becomes hot water of about 70 degreeC-73 degreeC, and is supplied to the heat generating power system G. As shown in FIG.

3 is a block diagram showing an outline of an internal configuration of the power generation system G. As shown in FIG. As the power generation system G, it is preferable to use a temperature difference power generation system that uses a low boiling point fluid such as ammonia, a pron, or an ammonia / water mixed fluid as the working fluid L. Such a temperature difference generation system itself is already known, for example, as described in Japanese Patent Application Laid-Open No. 7-91361 to Saga University Application. For example, temperature difference generation using a temperature difference between surface seawater and deep cold seawater having a relatively high temperature can be performed. It is a system that can be performed.

As shown in FIG. 3, the power generation system G includes a turbine 10, a generator 11, an absorber 12, a condenser 13, a circulation pump 14, a regenerator 15, and an evaporator 16. , The heater 17, the separator 18, the superheater (steam heater) 19, and the pressure reducing valve 20 are roughly configured. Moreover, this power generation system G also has the temperature sensors 21-24, the 1st control means 25, the 2nd control means 26, the 1st adjustment valve 27, and the 2nd adjustment valve 28. FIG. Have Since the working fluid L is circulated in the working fluid path R while repeating heating and cooling as shown in FIG. 3, the working fluid L is sequentially downstream from the circulation pump 14 (the direction in which the working fluid flows). Each configuration will be described in the direction of ()).

The liquid working fluid L sent out from the circulation pump 14 is preheated by the regenerator 15 and then sent to the evaporator 16. The position where this evaporator 16 is installed is the 3rd position in the working fluid path R. As shown in FIG. In this evaporator 16, the heat exchange of the working fluid L and the sewage drainage W is performed (third heat exchange step, the third heat exchange function), and the heat transfer from the sewage drainage W to the working fluid L is performed. All. As a result, the working fluid L becomes a gas-liquid two-phase state in which the internal heat energy state is raised, and is sent to the next heater 17.

The position where this heater 17 is provided is a 2nd position in the working fluid path R. As shown in FIG. In this heater 17, the heat exchange of the working fluid L and the hot air 2 is performed (second heat exchange step, the second heat exchange function), and the heat transfer from the hot air 2 to the working fluid L is performed. All. As a result, the working fluid L becomes the gas-liquid two-phase state which raised the internal thermal energy state further, and is sent to the separator 18. FIG.

The separator 18 separates the working fluid L in a gas-liquid two-phase state into a gas phase and a liquid phase. The working fluid L in the liquid phase portion is again sent to the regenerator 15 to dissipate heat, and then to the absorber 12 through the pressure reducing valve 20. On the other hand, the working fluid L in a gaseous state is sent from the separator 18 to the superheater 19. The position where the superheater 19 is provided is the first position in the working fluid path R. As shown in FIG. In this superheater 19, heat exchange between the working fluid L and the hot air 2 is carried out (first heat exchange step, first heat exchange function), whereby heat transfer from the hot air 2 to the working fluid L is performed. All. As a result, the working fluid L becomes superheated steam which raises the state of internal thermal energy further, and is sent to the turbine 10.

The working fluid L in the superheated steam state rotates the turbine 10 to generate power by a generator connected to the turbine 10. And the working fluid L which completed the electric power generation work joins the working fluid L which was sent to the absorber 12 and sent through the pressure reduction valve 20. The absorber 12 adopts, for example, a nozzle spray type, and the working fluid L (liquid phase) from the pressure reducing valve 20 is sprayed in the direction of the working fluid L (gas phase) in which power generation is completed. Heat is removed from the working fluid L and cooled.

Thereafter, the working fluid L sent to the condenser 13 is cooled by the cooling water C, returned to the liquid phase, and reaches the circulation pump 14 again. In this way, it is heated by the sewage drainage W and the hot air 2 while being sent by the circulation pump 14, and after being rotated by the turbine 10, is cooled by the cooling water C and then inside the path R. By circulating, the working fluid L generates electricity. The superheater 19 is installed in a first position upstream of the turbine 10 and downstream of the separator 18, and the heater 17 is installed in a second position upstream of the separator 18, and the evaporator 16 is provided in the 3rd position upstream from the heater 17. As shown in FIG.

The hot air 2 from the processing system S is aggregated from the plurality of processing systems S (hot air intensive step, hot air intensive function), and is sent to the power generation system G in an integrated state. Lose. Thereby, the influence of the fluctuation | variation of the processing situation for every processing system S is reduced, and the provision of the stable hot air 2 is attained.

The concentrated hot air 2 is first applied to the superheater 19 in the first position. Then, after that, it is applied to the heater 17 in the second position, and thereafter, it is applied to the drain heater 29 so that heat exchange with the sewage drainage W is performed (drainage heat exchange step, drainage heat exchange function). . Then, the hot air 2 after the completion of the heat exchange step for drainage is sent back to the treatment system S, and applied to the flue gas washing tower 105 of each treatment system S to be used as the anti-smoke smoke 2. have. The white smoke prevention air 2 is in contact with the exhaust gas (contact step, contact function) to prevent the generation of white smoke in the exhaust gas.

In the power generation system G, a superheater avoidance path 30 for avoiding application of the hot air 2 to the superheater 19 (first heat exchange avoidance step, first heat exchange avoidance function) is disposed, and the path 30 ), A first adjustment valve 27 is provided. The first regulating valve 27 opens or closes the valve based on the control signal from the first control means 25 to apply the hot air 2 to the superheater 19, or the superheater avoidance path. The application to the superheater 19 is avoided by leading to (30).

The first control means 25 is composed of, for example, a computer, a sequencer, a relay switch, and the like, and receives the sensor outputs of the temperature sensors 21 and 22, and based on these sensor outputs, the first control valve 27 is provided. Control opening and closing. The temperature sensor 21 measures the temperature t 1 of the working fluid L on the downstream side of the working fluid path R rather than the superheater 19 (first working fluid temperature measuring step, first working fluid temperature measuring function). For the sensor. In addition, the temperature sensor 22 measures the temperature T1 of the hot air 2 on the upstream side on the hot air 2 path than the superheater 19 (the first hot air temperature measuring step and the first hot air temperature measuring). Function).

More specifically, the first control means 25 is a high temperature applied to the superheater 19 based on the temperature difference between the measurement temperature T1 by the temperature sensor 22 and the measurement temperature t1 by the temperature sensor 21. The distribution of the gas amount of the air 2 and the gas amount of the hot air 2 that avoids the application to the superheater 19 is adjusted by the opening and closing control of the first adjustment valve 27. At this time, when the temperature difference T1-t1 between the temperature T1 and the temperature t1 is small, the first regulating valve 27 is opened to allow as much hot air 2 as possible to pass through the superheater avoidance path 30. When the temperature difference T1-t1 between the temperature T1 and the temperature t1 is large, the first adjustment valve 27 is closed to control as much hot air 2 as possible to pass through the superheater 19.

In the power generation system G, a heater avoidance path 31 for avoiding the application of the hot air 2 to the heater 17 (second heat exchange avoidance step, second heat exchange avoidance function) is disposed, and the path 31 The 2nd adjustment valve 28 is provided on (). The second regulating valve 28 opens or closes the valve based on the control signal from the second control means 26 to apply the hot air 2 to the heater 17, or the heater avoidance path. The application to the heater 17 is avoided by leading to (31).

The second control means 26 is composed of, for example, a computer, a sequencer, a relay switch, and the like, and receives the sensor outputs of the temperature sensors 23 and 24, and based on these sensor outputs, the second control valve 28 is provided. Control opening and closing. The temperature sensor 23 measures the temperature t2 of the working fluid L on the downstream side of the working fluid path R rather than the heater 17 (second working fluid temperature measuring step, second working fluid temperature measuring function). For the sensor. In addition, the temperature sensor 24 measures the temperature T2 of the hot air 2 on the upstream side (that is, downstream of the superheater 19) on the hot air 2 path than the heater 17 (the 2 high temperature air temperature measurement step, the second high temperature air temperature measurement function).

More specifically, the second control means 26 is a high temperature to be applied to the heater 17 based on the temperature difference between the measurement temperature T2 by the temperature sensor 24 and the measurement temperature t2 by the temperature sensor 23. Distribution of the gas amount of the air 2 and the gas amount of the hot air 2 which avoids application to the heater 17 is adjusted by the opening / closing control of the second adjustment valve 28. At this time, when the temperature difference T2-t2 between the temperature T2 and the temperature t2 is small, the second adjustment valve 28 is opened so that as much hot air 2 as possible passes through the heater avoidance path 31, When the temperature difference T2-t2 between the temperature T2 and the temperature t2 is large, the second adjustment valve 28 is closed to control as much hot air 2 as possible to pass through the heater 17.

The sewage drainage W from the processing system S is aggregated from the plurality of processing systems S (the sewage drainage concentration step, the sewage drainage concentration function), and is sent to the power generation system G in an integrated state. Lose. Thereby, the influence of the fluctuation | variation of the processing situation for every processing system S is reduced, and it is possible to provide stable sewage drainage W. As shown in FIG.

The concentrated sewage drainage W is configured to perform heat exchange with the hot air 2 after the second heat exchange step or the second heat exchange avoiding step in the drain heater 29 (drainage heat exchange step, drain heat exchange function). After that, the thin waste water W is applied to the evaporator 16 at the third position so that heat exchange with the working fluid L is performed (third heat exchange step, third heat exchange function).

As cooling water C which is a low temperature heat source, water of normal temperature can be used. The cooling water C applied to the condenser 13 is clean water, and the amount of water used can be suppressed by supplying water to the upper part of the flue gas washing tower 105 of the treatment system S after the condenser 13. Since the cooling water C is reused as the ductile waste water W, it contributes to the overall saving of the system and contributes to the improvement of the environmental aptitude. Since the cooling water C is also warmed by the condenser 13, when it is used for water supply to the flue gas washing tower 105, it contributes to the rise of the tower temperature, and has the effect of raising the temperature of the sewage drainage W.

Example

Example 1

The amount of power generation (turbine output) in the power generation system G of the structure shown in FIG. 4 was estimated by simulation calculation. Calculation conditions are as follows. In the first embodiment, the temperature T, the pressure p, the density index ρ, the ammonia / water ratio Y, and the entropy s of the working fluid L at the respective positions r1 to r10 on the working fluid path R shown in FIG. 4. And enthalpy H. The calculation results are shown in Table 1. Here, a density index value means the inverse of density (kg / m <3>).

<Calculation condition>

High temperature air (2):

Flow rate: 9300 ㎥ / h

Temperature at position g1: 300 ° C

Temperature at position g2: 170 ° C

Temperature at position g3: 150 ° C

Temperature at position g4: 100 ° C

ㆍ Seyeon drainage (W):

Flow rate: 53 ㎥ / h

Temperature at position w1: 70 ° C

Temperature at position w2: 60 ° C

Temperature at position w3: 73 ° C

ㆍ Coolant (C):

Temperature at position c1: 20 ° C

Temperature at position c2: 25 ° C

Working fluid (L):

Ingredients: ammonia / water ratio = 0.95

[Table 1]

Comparative Example 1

The amount of power generation (turbine output) in the power generation system G of the structure shown in FIG. 5 was estimated by simulation calculation. In this Comparative Example 1, the hot air 2 is not applied to the power generation system G, but the sewage drainage W (temperature at positions w1 and w2), the coolant C (temperature at positions c1 and c2) and The calculation conditions for the working fluid L are the same as in Example 1. In this comparative example 1, the temperature, the pressure, and the density of the working fluid L were estimated in each position r1-r10 on the working fluid path | route R shown in FIG. The calculation results are shown in Table 2. Here, a density index value means the inverse of density (kg / m <3>).

[Table 2]

Comparative Example 2

The power generation amount (turbine output) in the power generation system G of the structure shown in FIG. 6 was estimated by simulation calculation. The calculation conditions regarding the hot air 2 are as follows. The calculation conditions for the thin water drain W (temperature at positions w1 and w2), the coolant C (temperature at positions c1 and c2) and the working fluid L are the same as in Example 1. In this comparative example 2, the temperature, the pressure, and the density of the working fluid L were estimated in each position r1-r10 on the working fluid path | route R shown in FIG. Table 3 shows the results of the calculation. Here, a density index value means the inverse of density (kg / m <3>).

<Calculation condition>

High temperature air (2):

Flow rate: 9300 ㎥ / h

Temperature at position g1: 300 ° C

Temperature at position g2: 100 ° C

[Table 3]

[Comparative Example 3]

The power generation amount (turbine output) in the power generation system G of the structure shown in FIG. 7 was estimated by simulation calculation. The calculation conditions regarding the hot air 2 are as follows. The calculation conditions for the thin water drain W (temperature at positions w1 and w2), the coolant C (temperature at positions c1 and c2) and the working fluid L are the same as in Example 1. In this comparative example 3, the temperature, the pressure, and the density of the working fluid L were estimated in each position r1-r10 on the working fluid path | route R shown in FIG. The calculation results are shown in Table 4. Here, a density index value means the inverse of density (kg / m <3>).

<Calculation condition>

High temperature air (2):

Flow rate: 9300 ㎥ / h

Temperature at position g1: 300 ° C

Temperature at position g2: 100 ° C

[Table 4]

[Comparative Example 4]

The amount of power generation (turbine output) in the power generation system G of the structure shown in FIG. 8 was estimated by simulation calculation. The calculation conditions regarding the hot air 2 are as follows. The calculation conditions for the thin water drain W (temperature at positions w1 and w2), the coolant C (temperature at positions c1 and c2) and the working fluid L are the same as in Example 1. In this comparative example 4, the temperature, the pressure, and the density of the working fluid L were estimated in each position r1-r10 on the working fluid path | route R shown in FIG. Table 5 shows the results of the calculation. Here, a density index value means the inverse of density (kg / m <3>).

<Calculation condition>

High temperature air (2):

Flow rate: 9300 ㎥ / h

Temperature at position g1: 300 ° C

Temperature at position g2: 170 ° C

Temperature at position g3: 100 ° C

[Table 5]

As indicated above, the working fluid by applying the power generation system G (hot air 2) according to Embodiment 1 of the present invention to a first position downstream of the separator 18 and a second position upstream of the separator 18 Heat exchange with (L), and then apply the hot air (2) to the sewage drainage (W) to heat exchange with the sewage drainage (W), and again to the third position upstream than the second position. According to the configuration of heat exchange with the working fluid (L), the power generation efficiency can be remarkably improved. The turbine output (power generation amount) was improved by 181% over Comparative Example 1, 29% compared to Comparative Example 2, 26% compared to Comparative Example 3, and 0.6% compared to Comparative Example 4.

As mentioned above, although preferred embodiment of this invention was described, this invention is not limited to these, A various deformation | transformation and a change are possible within the range of the summary. For example, a plant arrangement, a hot spring heat, etc. can also be used instead of the heat retention gas discharged | emitted from an incinerator as reserve heat used for power generation.

C: Coolant G: Power Generation System (Array Power Generation System)
L: Working Fluid P: Plant (Sewage Treatment Plant)
R: working fluid path
S: Treatment system (sewage treatment system, incineration treatment system)
W: Water (segmented water, sewage drainage) 2: Hot air (white smoke prevention air)
10 turbine 11 generator
12 absorber 13 condenser
14: circulation pump 15: regenerator
16: evaporator 17: heater
18: Separator 19: Superheater (steam heater)
20: pressure reducing valve 21 to 24: temperature sensor
25 first control means 26 second control means
27: first regulating valve 28: second regulating valve
29: drain heater 30: superheater avoidance path
31: heater avoidance path 101: incinerator
102: flow air preheater 103: smoke prevention air preheater
104: dust collector 105: flue gas cleaning tower
106: nozzle 107: pump
108: chimney 109: shelf plate

Claims (10)

The hot air heated by the exhaust gas discharged from the incinerator of the incineration treatment system is generated upstream from the turbine in the working fluid path in a power generation system in which the turbine generates power by rotating the turbine by the working fluid and is lower than the separator. A first heat exchange step of performing heat exchange between the hot air at the first position and the working fluid by applying to the first position on the side;
Applying the hot air after the heat exchange at the first position to a second position upstream of the separator on the working fluid path, thereby performing heat exchange between the hot air at the second position and the working fluid. With two heat exchange stages,
A heat exchange step for drainage in which heat is exchanged between the duct waste water discharged from the incineration treatment system and the hot air after the heat exchange at the second position after the exhaust gas is cleaned;
Heat-exchanging the working fluid and the working fluid at the third position by applying the thin water drainage after the heat exchange with the hot air to a third position upstream of the second position on the working fluid path. A third heat exchange step,
A contacting step of bringing the hot air after heat exchange with the sewage drainage into contact with the exhaust gas as anti-smoke smoke
Array development method comprising a. The method of claim 1, further comprising: condensing the respective hot air from the plurality of incineration systems over the plurality of incineration systems before heat exchange at the first location;
Condensing said fine wastewater from said plurality of incineration treatment systems over said plurality of incineration treatment systems prior to heat exchange with said hot air.
Array development method further comprising. The first heat exchange avoiding step according to claim 1 or 2, wherein the hot air is joined with the hot air after heat exchange at the first position without applying the hot air to the first position;
A second heat exchange avoiding step of joining the hot air after the merging with the hot air after the heat exchange at the second position without applying to the second position
Array development method further comprising. The method of any one of claims 1 to 3, further comprising: measuring a first working fluid temperature of the working fluid after heat exchange at the first position;
Measuring a first hot air temperature of the hot air before heat exchange at the first position;
A first adjusting the distribution of the amount of hot air applied to the first position and the amount of hot air avoiding application to the first position based on the difference between the first hot air temperature and the first working fluid temperature Adjustment step,
Measuring a second working fluid temperature of the working fluid after heat exchange at the second position;
Measuring a second hot air temperature of the hot air before heat exchange at the second position;
A second adjusting the distribution of the amount of hot air applied to the second position and the amount of the hot air avoiding application to the second position based on the difference between the second hot air temperature and the second working fluid temperature; Adjustment steps
Array development method further comprising. Aggregating over each of said plurality of incineration treatment systems hot air heated by exhaust gas respectively discharged from a plurality of incinerators of a plurality of incineration treatment systems;
By applying the hot air after the aggregation to a first position upstream of the turbine in the working fluid path in the heat generating system in which the turbine generates power by rotating the turbine by the working fluid, the hot air at the first position A first heat exchange step of performing heat exchange of the working fluid,
A contacting step of bringing the hot air after the heat exchange at the first position into contact with the exhaust gas as anti-smoke smoke
Array development method comprising a. 6. The method of claim 5, wherein when the first position is downstream of the separator in the heat generating system,
Heat exchange of the hot air and the working fluid at the second position by applying the hot air after the first heat exchange step and before the contacting step to a second position upstream of the separator on the working fluid path And a second heat exchange step of carrying out the same. 7. The method of any one of claims 1 to 6, further comprising: applying coolant at a position downstream from the turbine in the working fluid path to cool the working fluid after rotating the turbine;
Contacting the exhaust gas with cooling water after cooling of the working fluid as fine water
Array development method further comprising. The process of any one of claims 1 to 7, wherein the working fluid is any of ammonia, prolon or ammonia / water mixed fluid. An array power generation system for generating power by rotating a turbine by a working fluid,
By applying the hot air heated by the exhaust gas discharged from the incinerator of the incineration treatment system to a first position upstream of the turbine and downstream of the separator on the working fluid path, the high temperature at the first position A first heat exchange function for performing heat exchange between air and the working fluid,
Applying the hot air after the heat exchange at the first position to a second position upstream of the separator on the working fluid path, thereby performing heat exchange between the hot air at the second position and the working fluid. 2 with heat exchange function,
A heat exchange function for drainage for performing heat exchange between the duct waste water discharged from the incineration treatment system and the hot air after the heat exchange at the second position after the exhaust gas is cleaned;
Heat-exchanging the working fluid and the working fluid at the third position by applying the thin water drainage after the heat exchange with the hot air to a third position that is upstream from the second position on the working fluid path. Third heat exchange function,
Contact function which makes the said high temperature air after heat exchange with the said waste water drainage contact with the said exhaust gas as a white smoke prevention air.
Array power generation system comprising a. An array power generation system for generating power by rotating a turbine by a working fluid,
A function of condensing each hot air heated by exhaust gas respectively discharged from a plurality of incinerators included in a plurality of incineration treatment systems over the plurality of incineration treatment systems;
A first heat exchange function for performing heat exchange between the hot air at the first position and the working fluid by applying the concentrated hot air to a first position upstream of the turbine on the working fluid path;
Contact function which makes the said high temperature air after heat exchange in a said 1st position contact with the said exhaust gas as a white smoke prevention air.
Array power generation system comprising a.

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