JPWO2011102408A1 - Waste heat recovery system and energy supply system - Google Patents

Abstract

An object of this invention is to improve the collection | recovery efficiency of effective energy rather than the exhaust heat recovery method by the production | generation of water vapor | steam. In order to achieve this object, in the present invention, a heat conduction path (1) through which exhaust heat is conducted and a high boiling point heating medium (R1) having an evaporation temperature higher than that of water (R3) are provided as a heat conduction path (1). A configuration is adopted in which a high-boiling-point heat medium steam generator (2) that generates high-boiling-point heat medium steam (R2) by exchanging heat with conducted exhaust heat is provided.

Description

The present invention relates to an exhaust heat recovery system, an energy supply system, and an exhaust heat recovery method.
Moreover, this invention claims priority based on Japanese Patent Application No. 2010-034776 for which it applied to Japan on February 19, 2010, and uses the content here.

As is well known, the energy efficiency of facilities is improved by recovering the heat of combustion exhaust gas (exhaust heat recovery) in various systems such as cogeneration systems, power generation systems such as thermal power plants, and steam generators such as boilers. Has been done. The following Patent Document 1 discloses an example of a cogeneration facility (system) using an exhaust heat recovery boiler, and the following Patent Document 2 discloses an example of a multi-pressure vertical natural circulation exhaust heat recovery boiler, Patent Document 3 below discloses an example of a combined cycle power plant that combines exhaust heat recovery boilers, and Patent Document 4 below discloses an example of a double pressure exhaust heat recovery boiler.

A cogeneration system is known as an energy supply system that uses exhaust heat generated during power generation to extract thermal energy used for air conditioning and hot water supply. In such a cogeneration system, as described in Patent Document 1, exhaust heat recovery by steam generation using an exhaust heat recovery boiler is generally performed.

Patent Document 5 discloses a waste heat recovery device that recovers waste heat (exhaust heat) from a relatively low-temperature heat source of about 200 ° C. using first and second working fluids having different boiling points. Yes. This waste heat recovery apparatus uses water as the first working fluid, and as the second working fluid, chlorofluorocarbon, hydrochlorofluorocarbon, hydrofluorocarbon, chlorofluorocarbon, hydrochlorofluorocarbon, hydrofluorocarbon, Ammonia or ammonia water is used, and more heat is recovered from a relatively low temperature heat source to improve power generation efficiency.

JP 2003-021302 A JP 2000-346303 A JP 2002-021583 A Japanese Patent No. 2753169 JP 2008-267341 A

However, the conventional exhaust heat recovery method by generating water vapor from the water described above does not necessarily have an effective energy recovery efficiency that can be recovered from the energy of the exhaust gas (exhaust heat). Further improvement is expected. In particular, in exhaust heat recovery from a relatively high temperature exhaust heat that greatly exceeds the evaporation temperature of water, for example, high temperature exhaust heat exceeding 300 ° C., there is a limit to the evaporation temperature when water is vaporized. However, the conventional exhaust heat recovery method does not have a sufficient effective energy recovery efficiency, and a large amount of effective energy is inevitably lost. The available energy is a thermodynamic concept also called exergy, and is generally known as energy that can be extracted as dynamic work from a certain system. The effective energy in the present invention means energy (work amount) that can be recovered as dynamic work (power such as electricity) in the total energy of the exhaust gas.
In addition, the conventional exhaust heat recovery method using water (first working fluid) and the second working fluid having a boiling point lower than that of the water is intended for heat recovery from a relatively low-temperature heat source of about 200 ° C. The temperature of the vapor obtained by vaporizing the second working fluid is lower than the temperature of the vapor obtained by vaporizing the first working fluid. Energy recovery is almost impossible.

The present invention relates to an exhaust heat recovery method for acquiring effective energy by vaporizing water, and more effective energy recovery than an exhaust heat recovery method for acquiring effective energy by vaporizing water and a liquid having a lower boiling point than the water. The objective is to improve efficiency.
Another object of the present invention is to provide an energy supply system that has higher efficiency, energy saving rate, and CO2 reduction rate than conventional ones.

In order to achieve the above object, in the present invention, as a means for solving the exhaust heat recovery system, a heat conduction path through which exhaust heat is conducted and a high boiling point heat medium having a higher evaporation temperature than water are conducted through the heat conduction path. A high-boiling-point heat medium steam generator that generates high-boiling-point heat medium steam by exchanging heat with exhaust heat is employed.

According to the present invention, instead of vaporizing water to produce water vapor, or in addition to vaporizing water to produce water vapor, the evaporation temperature is higher than water (vapor pressure is lower than water). Since the high-boiling point heat medium is evaporated to generate the high-boiling point heat medium vapor, it is possible to improve the recovery efficiency of the effective energy as compared with the conventional exhaust heat recovery method in which water is evaporated to generate water vapor.

It is a system configuration figure showing the functional composition of energy supply system P1 concerning a 1st embodiment of the present invention. It is a characteristic view which shows the heat exchange state of each heat medium in the exhaust heat recovery part K1 of the energy supply system P1 which concerns on 1st Embodiment of this invention with the relationship between the amount of exchange heat (horizontal axis) and temperature (vertical axis). It is a system block diagram which shows the function structure of the energy supply system P2 which concerns on 2nd Embodiment of this invention. It is a characteristic view which shows the heat exchange state of each heat medium in the exhaust heat recovery part K2 of the energy supply system P2 which concerns on 2nd Embodiment of this invention by the relationship between the amount of exchange heat (horizontal axis) and temperature (vertical axis). In 2nd Embodiment of this invention, it is a characteristic view which shows the energy-saving rate in the case where ethylene glycol is employ | adopted as a high boiling-point heating medium R1, and the case where diethylene glycol is employ | adopted. In a second embodiment of the present invention, it is a characteristic diagram showing the CO ₂ reduction rate in the case of a high-boiling heat transfer medium R1 employing the case and diethylene glycol is employed ethylene glycol. It is a system block diagram which shows the function structure of the energy supply system P3 which concerns on 3rd Embodiment of this invention. It is a characteristic view which shows the heat exchange state of each heat medium in the exhaust heat recovery part K3 of the energy supply system P3 which concerns on 3rd Embodiment of this invention by the relationship between the amount of exchange heat (horizontal axis) and temperature (vertical axis).

Embodiments of the present invention will be described below with reference to the drawings.
[First Embodiment]
First, a first embodiment of the present invention will be described with reference to FIG. 1 and FIG.
As shown in FIG. 1, the energy supply system P <b> 1 according to the first embodiment includes an exhaust gas pipe 1, a high boiling point heat medium steam generator 2, a steam generator 3, a high boiling point heat medium preheater 4, and a water preheater 5. , High boiling point heat medium steam superheater 6, steam superheater 7, high boiling point heat medium supply pump 8, feed water pump 9, high boiling point heat medium steam turbine generator 10, high boiling point heat medium steam condenser 11, condensate tank 12 The steam turbine generator 13, the steam condenser 14, the condensate tank 15, and the cooling water supply device 16 are configured. In FIG. 1, reference numeral G denotes a high temperature exhaust gas, R1 denotes a high boiling point heating medium, R2 denotes a high boiling point heating medium vapor, R3 denotes water, and R4 denotes water vapor.

Among these components, the exhaust gas pipe 1, the high boiling point heat medium steam generator 2, the steam generator 3, the high boiling point heat medium preheater 4, the water preheater 5, the high boiling point heat medium steam superheater 6, and the steam superheater. 7 constitutes an exhaust heat recovery section K1 for recovering exhaust heat from the high temperature exhaust gas G. The exhaust heat recovery unit K1 corresponds to the exhaust heat recovery system according to the present invention.

Among the above components, the high boiling point heat medium supply pump 8, the feed water pump 9, the high boiling point heat medium steam turbine generator 10, the high boiling point heat medium steam condenser 11, the condensate tank 12, and the steam turbine generator 13. The steam condenser 14, the condensate tank 15 and the cooling water supply device 16 constitute an electric power generation unit W. The power generation unit W supplies the high-boiling point heat medium R1 and water R3, which are liquid heat media, to the exhaust heat recovery unit K1, and the high-boiling point heat medium vapor R2 and water vapor that are vaporized by the above-described exhaust heat. This is a power generation unit that recovers R4 from the exhaust heat recovery unit K1 and generates electric power (power) using the high boiling point heat medium vapor R2 and the water vapor R4 as working fluids. The energy supply system P1 composed of the exhaust heat recovery unit K1 and the power generation unit W (power generation unit) is a high-boiling-point heat transfer steam generated by recovering exhaust heat from the high-temperature exhaust gas G in the exhaust heat recovery unit K1. This is an electric power generation system that generates electric power that is one form of power by R2 and water vapor R4.

In such an energy supply system P1, the exhaust gas pipe 1 is a heat conduction path through which the high-temperature exhaust gas G supplied from the outside flows. The high-temperature exhaust gas G is, for example, high-temperature exhaust gas discharged from the combustor (that is, gas having exhaust heat), and a temperature that is significantly higher than the temperature required for vaporizing the water R3, for example, a temperature of 300 ° C. or higher. Have Such high-temperature exhaust gas G flows from the left side (upstream side) to the right side (downstream side) of the exhaust gas pipe 1 as shown in FIG.

As shown in FIG. 1, the high-boiling-point heat medium steam generator 2 is provided in the middle of the exhaust gas pipe 1, and by exchanging heat between the high-boiling point heat medium R1 and the high-temperature exhaust gas G, This is a device for generating the medium vapor R2. Further, as shown in FIG. 1, the steam generator 3 is provided in the exhaust gas pipe 1 on the downstream side of the high-boiling-point heat medium steam generator 2, and the water R3 is exchanged with the high-temperature exhaust gas G for high pressure. Is an apparatus (boiler) for generating water vapor R4.

Here, the high boiling point heating medium R1 is a liquid of a compound that has a higher evaporation temperature than water R3 (that is, a vapor pressure lower than that of water R3) and is chemically stable in heat exchange with the high-temperature exhaust gas G. For example, ethylene glycol (molecular formula: C ₂ H ₆ O ₂ ), diethylene glycol (molecular formula: C ₂ H ₁₀ O ₃ ), propylene glycol (C ₃ H ₈ O ₂ ), triethylene glycol (molecular formula: C ₆ H ₁₄ O) ₄ ), propylene carbonate (molecular formula: C ₄ H ₅ O ₃ ), propylene ethylene glycol (molecular formula: C ₃ H ₈ O ₂ ), formamide (molecular formula: CH ₃ NO), and the like.

As shown in FIG. 1, the high boiling point heat medium preheater 4 is provided between the high boiling point heat medium steam generator 2 and the steam generator 3 in the exhaust gas pipe 1. This high boiling point heat medium preheater 4 is a kind of heat exchange that preheats to a temperature just before boiling, for example, by exchanging the high boiling point heat medium R1 supplied from the high boiling point heat medium supply pump 8 with the high temperature exhaust gas G. The high-boiling point heating medium R1 preheated is discharged to the high-boiling point heating medium steam generator 2.

As shown in FIG. 1, the water preheater 5 is provided on the downstream side of the steam generator 3 in the exhaust gas pipe 1. This water preheater 5 is a kind of heat exchanger that preheats the water R3 supplied from the feed water pump 9 to the temperature just before boiling, for example, by exchanging heat with the high-temperature exhaust gas G. It discharges to the generator 3 and the high-boiling-point heat medium steam condenser 11.

As shown in FIG. 1, the high boiling point heat medium steam superheater 6 is provided upstream of the high boiling point heat medium steam generator 2 in the exhaust gas pipe 1. The high boiling point heat medium steam superheater 6 is a kind of heat exchanger that superheats by exchanging heat between the high boiling point heat medium steam R2 supplied from the high boiling point heat medium steam generator 2 and the high temperature exhaust gas G. The high boiling point heat medium steam R2 is discharged to the high boiling point heat medium steam turbine generator 10.

As shown in FIG. 1, the steam superheater 7 is provided upstream of the high-boiling-point heat medium steam superheater 6 in the exhaust gas pipe 1. The steam superheater 7 is a kind of heat exchanger that superheats the steam R4 supplied from the steam generator 3 and the high-boiling-point heat medium steam condenser 11 by exchanging heat with the high-temperature exhaust gas G. Is discharged to the steam turbine generator 13.

The high boiling point heating medium supply pump 8 is a pump that pumps out the high boiling point heating medium R 1 from the condensate tank 12 and supplies it to the high boiling point heating medium preheater 4. The water supply pump 9 is a pump that pumps water R3 from the condensate tank 15 and supplies it to the water preheater 5. The high boiling point heat medium steam turbine generator 10 rotates the turbine using the high pressure high boiling point heat medium steam R2 supplied from the high boiling point heat medium steam generator 2 via the high boiling point heat medium steam superheater 6. Thus, a turbine generator that generates electric power by driving a generator axially coupled to the turbine.

The high-boiling point heat medium steam condenser 11 exchanges heat with the water R3 supplied from the water preheater 5 for the high-boiling point heat medium steam R2 after power recovery discharged from the turbine of the high-boiling point heat medium steam turbine generator 10. This is a kind of heat exchanger that condenses (liquefies) the high-boiling-point heat transfer medium vapor R2 to restore the high-boiling-point heat transfer medium R1, and vaporizes the water R3 to form the high-pressure steam R4. The high boiling point heat medium steam condenser 11 discharges the restored high boiling point heat medium R1 to the condensate tank 12, while the steam R4 generated by heat exchange with the high boiling point heat medium steam R2 is supplied to the steam superheater 7. Discharge.

The condensate tank 12 is a storage tank that temporarily stores the high boiling point heat medium R1 supplied from the high boiling point heat medium vapor condenser 11. The steam turbine generator 13 is axially coupled to the turbine by rotating the turbine using the high-pressure steam R 4 supplied from the steam generator 3 and the high-boiling-point heat medium steam condenser 11 via the steam superheater 7. This is a turbine generator that generates electricity by driving a generator.

The steam condenser 14 condenses (liquefies) water R3 by exchanging heat from the steam R4 after power recovery discharged from the turbine of the steam turbine generator 13 with the cooling water supplied from the cooling water supply device 16. It is a kind of heat exchanger that is restored to Such a steam condenser 14 discharges the restored water R3 to the condensate tank 15. The condensate tank 15 is a storage tank that temporarily stores the water R3 supplied from the steam condenser 14. The cooling water supply device 16 is a device that circulates and supplies the cooling water to the steam condenser 14.

Next, the operation of the energy supply system P1 according to the first embodiment will be described in detail with reference to the characteristic diagram of FIG.

In the energy supply system P1, as shown in FIG. 1, a plurality of heat exchangers that exchange heat with the high-temperature exhaust gas G are arranged from the upstream side to the downstream side of the exhaust gas pipe 1, that is, in the axial direction of the exhaust gas pipe 1. . That is, among the heat exchangers, the steam superheater 7 is located in the uppermost stream of the exhaust gas pipe 1, and the high boiling point heat medium steam superheater 6 → the high boiling point heat medium steam generator 2 is disposed downstream of the steam superheater 7. → The high boiling point heating medium preheater 4 → the steam generator 3 → the water preheater 5 are arranged in this order. Therefore, the high-temperature exhaust gas G flowing through the region (heat exchange region) of the exhaust gas pipe 1 in which these heat exchangers are disposed deprives each heat exchanger of heat by passing through the heat exchange region from the upstream side to the downstream side. Therefore, the temperature is higher at the upstream side of the heat exchange region (the temperature is lower at the downstream side).

Focusing on the high boiling point heat medium steam generator 2 and the steam generator 3, the high boiling point heat medium steam generator 2 is located upstream of the steam generator 3 in the heat exchange region. The high boiling point heating medium R1 in the generator 2 exchanges heat with the high-temperature exhaust gas G that is higher in temperature than the water R3 in the steam generator 3.

FIG. 2 shows the heat exchange state of each heat medium (that is, the high temperature exhaust gas G, the high boiling point heat medium R1, the high boiling point heat medium steam R2, the water R3, and the water vapor R4) in the heat exchange region and the heat exchange amount (horizontal axis) and the temperature. It is a characteristic view shown by the relationship with (vertical axis). In FIG. 2, a solid line Lg indicates a change in the state of the high-temperature exhaust gas G, a broken line Ls indicated by a one-dot chain line indicates a change in the state of water R3 or water vapor R4, and a broken line Lk indicated by a dotted line indicates the high boiling point heating medium R1. Or the state change of high boiling-point heat-medium vapor | steam R2 is shown.

As shown in FIG. 2, since the high-temperature exhaust gas G is deprived of heat by each heat exchanger, the relationship between the exchange heat and temperature is almost proportional as shown by a line Lg. That is, in this characteristic diagram, the exchange heat amount point A1 corresponds to the most downstream point in the heat exchange region, and the exchange heat amount point C3 corresponds to the most upstream point in the heat exchange region. And each heat exchanger is located between the exchange heat amount point A1 (the most downstream point) to the exchange heat amount point C3 (the most upstream point) in heat exchange characteristics, and performs heat exchange using the high temperature exhaust gas G as a heat source.

Looking at the heat exchange between the water R3 and the steam R4 and the high temperature exhaust gas G, that is, the heat exchange in the water preheater 5, the steam generator 3 and the steam superheater 7, the water R3 is preheated by the water preheater 5. It is distributed and supplied to the steam generator 3 and the high boiling point heat medium steam condenser 11. Some of the water R3 is converted into water vapor R4 by heat exchange with the high-temperature exhaust gas G in the water vapor generator 3, and the remaining water R3 is exchanged with high boiling point heat medium steam R2 in the high boiling point heat medium steam condenser 11. It becomes water vapor R4.

The area of the exchange heat points A1 to A2 in the broken line Ls corresponds to the temperature rise (pressurization) up to the temperature just before the boiling point of the water R3 by the water preheater 5, and the area of the exchange heat points A2 to B1 in the broken line Ls is the same. This corresponds to the vaporization of a part of water R3 (steam R4) by the steam generator 3. Moreover, the area | region of the exchange-heat amount point B1-D in the broken line Ls is corresponded to vaporization (water vapor | steam R4 conversion) of the remaining water R3 by the high boiling-point heat-medium vapor | steam condenser 11. FIG. That is, the water R3 preheated to a temperature just before the boiling point by the water preheater 5 becomes steam R4 due to the exchange heat quantity over the exchange heat quantity points A2 to D.

Then, the water vapor R 4 discharged from the water vapor generator 3 and the water vapor R 4 discharged from the high-boiling-point heat medium vapor condenser 11 join together and are supplied to the water vapor superheater 7. That is, the water vapor R4 generated in the water vapor generator 3 and the high-boiling-point heat medium vapor condenser 11 becomes water vapor R4 (superheated water vapor) superheated to the boiling point by heat exchange with the high-temperature exhaust gas G in the water vapor superheater 7. . The region of the exchange heat quantity points C2 to C3 in the broken line Ls is a superheated region of the steam R4 by the steam superheater 7. Note that the temperature of the exchange heat amount point C2 corresponding to the overheating start point of the water vapor R4 is equal to the temperature of the exchange heat amount point D (vaporization end point) of the water vapor R4 as shown in the figure.

On the other hand, heat exchange between the high boiling point heating medium R1 and the high boiling point heating medium steam R2 and the high temperature exhaust gas G, that is, the high boiling point heating medium preheater 4, the high boiling point heating medium steam generator 2, and the high boiling point heating medium steam superheater. 6, the high boiling point heating medium R1 is preheated to a temperature just before the boiling point by heat exchange with the high temperature exhaust gas G in the high boiling point heating medium preheater 4, and then the high boiling point heating medium vapor is heated. It is supplied to the generator 2 to become a high boiling point heating medium vapor R2. The region of exchange heat quantity points B1 to B2 in the polygonal line Lk corresponds to the temperature rise (pressurization) up to the temperature just before the boiling point of the high boiling point heating medium R1 by the high boiling point heating medium preheater 4, and the exchange heat point in the polygonal line Lk as well. The region of B2 to C1 corresponds to vaporization of the high boiling point heat medium R1 (high boiling point heat medium steam R2) by the high boiling point heat medium steam generator 2.

The high-boiling-point heat transfer steam R2 discharged from the high-boiling-point heat transfer steam generator 2 is superheated above the boiling point by heat exchange with the high-temperature exhaust gas G in the high-boiling-point heat transfer steam superheater 6. R2 (superheated high boiling point heating medium vapor). The region of the exchange heat quantity points C1 to C2 in the polygonal line Lk is a superheated region of the high boiling point heat medium steam R2 by the high boiling point heat medium steam superheater 6.

Here, the high boiling point heating medium R 1 supplied to the high boiling point heating medium preheater 4 by the high boiling point heating medium supply pump 8 is discharged from the high boiling point heating medium steam turbine generator 10 in the high boiling point heating medium steam condenser 11. The high boiling point heating medium vapor R2 is liquefied by heat exchange with the water R3 discharged from the water preheater 5. The heat exchange in the high-boiling-point heat medium vapor condenser 11 corresponds to a region of exchange heat amount points D to B1 on the polygonal line Lk.

In the region of the exchange heat points D to B1 on the polygonal line Lk, the heat of the heat exchange initially acts as sensible heat on the high-boiling-point heat medium steam R2, whereby the temperature of the high-boiling-point heat medium steam R2 gradually decreases. Thereafter, the heat acts as latent heat on the high-boiling-point heat medium steam R2, so that a constant amount of the high-boiling-point heat medium steam R2 is condensed while maintaining a constant value. Such a state change of the high boiling point heating medium vapor R2 relates to the case where the high boiling point heating medium R1 is ethylene glycol (molecular formula: C ₂ H ₆ O ₂ ), and varies depending on the type of the high boiling point heating medium R1.

That is, in the exhaust heat recovery unit K1 of the energy supply system P1, the water R3 in the state Ys corresponding to the exchange heat quantity point A1 is heated with the high temperature exhaust gas G having a relatively low temperature in the water preheater 5 and the steam generator 3. As a result of the exchange and heat exchange with the high-boiling-point heat medium steam R2 (high-boiling-point heat medium steam) in the high-boiling-point heat medium steam condenser 11 and heat exchange with the high-temperature exhaust gas G at a relatively high temperature in the steam superheater 7, The steam R4 in the state Xs is heated to a temperature corresponding to the exchange heat quantity point C3. Then, the steam R4 in the state Xs is supplied to the steam turbine generator 13 as a power source and released, and then cooled, condensed and condensed, and returns to the water R3 in the state Ys corresponding to the exchange heat quantity point A1. .

In the exhaust heat recovery unit K1, the high boiling point heat medium R1 in the state Yk corresponding to the exchange heat quantity point D is the high boiling point heat medium preheater 4, the high boiling point heat medium steam generator 2, and the high boiling point heat medium steam superheated. By the heat exchange with the high-temperature exhaust gas G having a relatively high temperature in the vessel 6, the high-boiling-point heat transfer steam R2 in the state Xk is heated to a temperature corresponding to the exchange heat point C2 of the broken line Lk. The high-boiling-point heat medium steam R2 in the state Xk is supplied to the high-boiling-point heat medium steam turbine generator 10 as a power source and released, thereby releasing the high-boiling point heat medium in the state YL corresponding to the exchange heat point D. Return to R1.

According to such an exhaust heat recovery unit K1, in addition to exhaust heat recovery by vaporizing water R3 by heat exchange with the high temperature exhaust gas G to form water vapor R4, the evaporation temperature is higher than that of water R3 by heat exchange with the high temperature exhaust gas G. The high-boiling point heat medium R1 is vaporized to a high-boiling point heat medium steam R2 by vaporizing the high boiling point heat medium R1 (which has a lower vapor pressure than the water R3), so that the effective energy recovery efficiency is improved over conventional exhaust heat recovery methods. It is possible to make it.

That is, by applying the high boiling point heating medium R1, a Rankine cycle in which power is extracted by an enthalpy difference between the state Xk (gas phase) and the state YL (gas phase or gas-liquid mixed phase) can be constructed, but the boiling point is higher than that of the water R3. In a low boiling point heating medium (conventional chlorofluorocarbon or alternative chlorofluorocarbon) having a low temperature, the high temperature range exceeds the critical point, and power cannot be taken out by Rankine cycle. That is, according to the exhaust heat recovery unit K1, by using the high boiling point heating medium R1, it is possible to efficiently extract effective energy in a high temperature range that is impossible with a low boiling point heating medium.

Further, according to the exhaust heat recovery section K1, the high boiling point heat medium steam R2 is superheated using the high boiling point heat medium steam superheater 6 and the steam R4 is superheated using the steam superheater 7, so that heat recovery is possible. The efficiency can be further improved as compared with the conventional exhaust heat recovery method.

[Second Embodiment]
Next, a second embodiment of the present invention will be described with reference to FIGS.
In FIG. 3, the same components as those of the energy supply system P1 according to the first embodiment shown in FIG.

The energy supply system P2 according to the second embodiment includes an exhaust heat recovery unit K2 and a power generation / steam output unit W2, and as shown in FIG. 3, the energy supply system according to the first embodiment described above. The steam superheater 7, the steam turbine generator 13, the steam condenser 14, the condensate tank 15, and the cooling water supply device 16 are deleted from P1. That is, in this energy supply system P2, the water vapor R4 discharged from the water vapor generator 3 and the water vapor R4 discharged from the high-boiling-point heat medium vapor condenser 11 are merged and supplied to the external water vapor load. The condensate recovered from is input to the feed pump 9.

In this energy supply system P2, as shown in FIG. 3, the exhaust heat recovery unit K2 includes the exhaust gas pipe 1, the high-boiling-point heat medium steam generator 2, the steam generator 3, It consists of a boiling point heat medium preheater 4, a water preheater 5, and a high boiling point heat medium steam superheater 6. The power generation / steam output section W2 is composed of a high boiling point heat medium supply pump 8, a feed water pump 9, a high boiling point heat medium steam turbine generator 10, a high boiling point heat medium steam condenser 11 and a condensate tank 12. Yes.

The heat exchange state of each heat medium (high temperature exhaust gas G, high boiling point heat medium R1, high boiling point heat medium steam R2, water R3 and water vapor R4) in the heat exchange region of such exhaust heat recovery section K2 is shown in FIG. It becomes. That is, when the heat exchange between the water R3 and the water vapor R4 and the high temperature exhaust gas G, that is, the heat exchange in the water preheater 5 and the water vapor generator 3, the water R3 in the state Ys1 corresponding to the exchange heat quantity point Aa is broken. As shown by Ls1, heat exchange with the high temperature exhaust gas G at a relatively low temperature in the water preheater 5 preheats to the exchange heat point Ab, which is a temperature just before the boiling point, and further the high temperature in the steam generator 3 The heat exchange with the exhaust gas G and the heat exchange with the high boiling point heat medium vapor R2 (high boiling point heat medium vapor) in the high boiling point heat medium vapor condenser 11 result in the water vapor R4 in the state Xs1 corresponding to the exchange heat quantity point Da. Then, the water vapor R4 in the state Xs1 is supplied as a heat source to the external heat load, and returns to the water R3 in the state Ys1 corresponding to the exchange heat amount point Aa by releasing energy by the external heat load.

On the other hand, the high boiling point heating medium R1 in the state Yk1 corresponding to the exchange heat point B1 is exchanged with the high temperature exhaust gas G having a relatively high temperature in the high boiling point heating medium preheater 4 and the high boiling point heating medium steam generator 2, The high boiling point heat medium steam R2 is in a state corresponding to the exchange heat point C1 of the polygonal line Lk1, and the high boiling point heat medium steam R2 is superheated above the boiling point by heat exchange with the high temperature exhaust gas G in the high boiling point heat medium steam superheater 6. It becomes the high boiling point heating medium vapor R2 (superheated high boiling point heating medium vapor) of the state Xk1. The high boiling point heating medium steam R2 (superheated high boiling point heating medium steam) in the state Xk1 is supplied to the high boiling point heating medium steam turbine generator 10 as drive power and discharged, thereby corresponding to the exchange heat point Da. It returns to the high boiling point heating medium R1 in the state YL1.

That is, this energy supply system P2 is a cogeneration system that supplies electric energy to the outside and supplies heat energy by water vapor to the outside. According to the exhaust heat recovery unit K2 of the present energy supply system P2, the water R3 is exchanged by heat exchange with the high temperature exhaust gas G in the same manner as the exhaust heat recovery unit K1 of the energy supply system P1 according to the first embodiment described above. In addition to recovering exhaust heat from steam R4, high-boiling point heat medium R1 has a higher evaporation temperature than water R3 (has a lower vapor pressure than water R3) due to heat exchange with high-temperature exhaust gas G. Therefore, the effective energy recovery efficiency can be improved as compared with the conventional exhaust heat recovery method.

Here, when ethylene glycol (molecular formula: C ₂ H ₆ O ₂ ) is employed as the high boiling point heating medium R 1 and diethylene glycol (molecular formula: C ₂ H ₁₀ O ₃ ) is employed, the total efficiency is estimated. Is 81.26% (= 30.56% (power generation efficiency) + 50.70% (waste heat recovery efficiency)), and in the case of diethylene glycol, it is 80.66% (= 33.15% (power generation efficiency) +47. 56% (exhaust heat recovery efficiency)).

That is, when ethylene glycol is used, the overall efficiency is slightly higher than when diethylene glycol is used, but the power generation efficiency is higher when diethylene glycol is used than when ethylene glycol is used. Such a difference in power generation efficiency is attributed to the pressure difference between the gas and liquid of both heat carriers. Under the same temperature condition, for example, when the gas pressure of both heating media is 1.5 MPa, the liquid pressure of ethylene glycol is 0.109 MPa, whereas the liquid pressure of diethylene glycol is 0.027 MPa. That is, since diethylene glycol has a lower liquid pressure than ethylene glycol, diethylene glycol has a greater gas-liquid pressure difference than ethylene glycol. This difference in gas-liquid pressure difference is the cause of power generation efficiency.

Further, FIG. 5 shows energy saving rates when ethylene glycol is used as the high boiling point heating medium R1 and when diethylene glycol is used. FIG. 5 is a characteristic diagram in which the horizontal axis is the power generation end thermal efficiency η _{E based} on the low calorific value (LHV) and the vertical axis is the exhaust heat recovery efficiency η _H , and the energy saving efficiency η _S1 when ethylene glycol is used and The energy saving efficiency η _S2 when diethylene glycol is used is shown. As shown in FIG. 5, the energy saving efficiency η _S1 is 23.5%, whereas the energy saving efficiency η _S2 is 25.1%. When diethylene glycol is used, ethylene glycol is used. A slightly higher value.

Further, FIG. 6 shows the CO ₂ reduction rate when ethylene glycol is used as the high boiling point heating medium R1 and when diethylene glycol is used. FIG. 6 is a characteristic diagram with the heat generation end thermal efficiency ηE based on the low calorific value (LHV) as the horizontal axis and the exhaust heat recovery efficiency ηH as the vertical axis, and the CO ₂ reduction rate S ₁ when ethylene glycol is used and This shows the CO ₂ reduction rate S2 when diethylene glycol is used. As shown in FIG. 6, the CO ₂ reduction rate S ₁ is 38.4%, whereas the CO ₂ reduction rate S ₂ is 40.4%, and diethylene glycol is used in the same manner as the energy saving rate described above. When this is done, the value is slightly higher than when ethylene glycol is used.

The energy supply system P2 is a cogeneration system that supplies electric energy to the outside and supplies heat energy from water vapor to the outside. The energy supply system P2 collects exhaust heat from the exhaust gas like the energy supply system P1 of the first embodiment. The energy supply device that converts the available energy obtained from the above into electric energy and supplies it as power, or the energy that is converted into only heat energy and supplied to the outside as steam, such as a well-known exhaust heat recovery boiler Different from the feeding device. In these energy supply devices, available energy is converted into a single energy such as electric energy or heat energy, so that a high energy saving rate and CO ₂ reduction rate cannot be achieved as in the case of the energy supply system P2.

[Third Embodiment]
Next, a third embodiment of the present invention will be described with reference to FIGS. In FIG. 7, the same components as those of the energy supply system P2 according to the second embodiment shown in FIG.

As shown in FIG. 7, the energy supply system P3 according to the third embodiment is mainly characterized in that the steam generator 3 is replaced with a flash tank 17 in the energy supply system P2 according to the second embodiment. . The energy supply system P3 further includes a pressurizing pump 18 as a component accompanying the flash tank 17.

That is, the exhaust heat recovery unit K3 in the energy supply system P2 includes an exhaust gas pipe 1, a high boiling point heat medium steam generator 2, a high boiling point heat medium preheater 4, a water preheater 5, a high boiling point heat medium steam superheater 6, and It is composed of a flash tank 17. The power generation / steam output unit W3 includes a high boiling point heat medium supply pump 8, a feed water pump 9, a high boiling point heat medium steam turbine generator 10, a high boiling point heat medium steam condenser 11, a condensate tank 12, and a pressure pump. It is comprised from 18.

The flash tank 17 is a flash-type steam generator that steams water (high-temperature high-pressure water) supplied from the water preheater 5 by a flash phenomenon. This flash tank 17 is a kind of container in which the internal pressure is adjusted so that the water (high-temperature high-pressure water) supplied from the water preheater 5 is vaporized by the flash phenomenon, and the steam R4 (flash steam) and the saturated water R5. And generate The flash phenomenon is known as a phenomenon in which a part of the high-temperature high-pressure water is vaporized as saturated water vapor when the pressure is released by releasing the high-temperature high-pressure water into a low-pressure atmosphere.

The pressurizing pump 18 is a pump that pressurizes water recovered from an external heat load. The water discharged from the pressurizing pump 18 is distributed and supplied to the feed water pump 9 and the high boiling point heat medium steam condenser 11. Further, the water vapor R4 generated in the flash tank 17 is supplied to an external heat load, and the saturated water R5 similarly generated in the flash tank 17 is a water supply pump discharged from a pressurizing pump 18 as shown in the figure, for example. 9 is distributed to the feed water pump 9 and the high-boiling-point heat medium steam condenser 11 by being supplied to the branch point j between the high-boiling-point heat medium steam condenser 11.

That is, this energy supply system P3 has a pressure (reduced pressure) instead of the steam generator 3 of the second embodiment that generates the steam R4 by the action of heat obtained by heat exchange between the water R3 and the high temperature exhaust gas G. ) Is provided with a flash tank 17 that generates water vapor R4.

Since the pressure of the water recovered from the external heat load is lower than the pressure of the saturated water R5 output from the flash tank 17, if the pressurizing pump 18 is not provided, a high boiling point heat medium steam condenser is provided. 11 becomes difficult to supply water with a sufficient pressure, and the supply efficiency of water vapor R4 to the outside decreases. Therefore, the pressure pump 18 is not an essential component of the third embodiment, but is preferably provided.

FIG. 8 shows the heat exchange state of each heat medium (high-temperature exhaust gas G, high-boiling-point heat medium R1, high-boiling-point heat medium steam R2, water R3, and water vapor R4) in the exhaust heat recovery unit K3 of the energy supply system P3. Indicates. As shown by the broken line Ls2 in FIG. 8, the water R3 can be preheated in a region extending from the exchange heat amount points Aa to B1, that is, a region wider than the region extending from the exchange heat amount points Aa to Ab of the second embodiment.

The heat exchange between the water R3 and the high-temperature exhaust gas G in the region extending over the exchange heat quantity points Aa to B1 is more effective energy as can be seen from comparison with FIG. 4 showing the heat exchange state of the second embodiment. Can be obtained from the high temperature exhaust gas G. Therefore, according to the third embodiment, since a larger amount of water R3 can be preheated, it is possible to generate a larger amount of water vapor R4 than in the second embodiment. Further, according to the third embodiment, since the flash tank 17 is used in place of the steam generator 3, the cost of the system can be reduced.

In addition, this invention is not limited to said each embodiment, For example, the following modifications can be considered.
(1) In each of the above embodiments, in addition to two types of liquids having different vapor pressures, that is, water R3, the high-boiling point heat medium R1 having a vapor pressure lower than that of the water R3 is used for heat recovery of the exhaust heat of the high-temperature exhaust gas G. However, instead of this, the exhaust heat of the high temperature exhaust gas G may be recovered by using only the high boiling point heating medium R1 or using three or more kinds of liquids having different vapor pressures.

For example, when the exhaust heat of the high-temperature exhaust gas G is recovered using only the high-boiling heat medium R1, heat exchange with a smaller temperature difference is possible than when the water R3 is used, depending on the temperature of the high-temperature exhaust gas G. Therefore, the effective energy recovery efficiency can be improved as compared with the case where only the conventional water R3 is used. Further, in addition to the high boiling point heating medium R1 and the water R3, a low boiling point heating medium having a lower boiling point than the water R3 may be combined to recover the exhaust heat of the high temperature exhaust gas G.

(2) In the first and second embodiments, the high-boiling-point heat medium preheater 4 and the water preheater 5 are constituent elements. However, although the heat recovery efficiency is reduced, the high-boiling point heat medium preheater is used as necessary. 4 and the water preheater 5 may be omitted.

(3) Although each said embodiment is related with the case where heat recovery of the exhaust heat of the high temperature exhaust gas G is concerned, the heat source (exhaust heat) used as the object of heat recovery is not limited to the high temperature exhaust gas G (gas). For example, it may be a high-temperature liquid or solid exceeding 300 ° C. Therefore, the heat conduction path in the present invention is not limited to the exhaust gas pipe 1 through which the high-temperature exhaust gas G (gas) flows.

(4) In the above embodiments, the high-boiling-point heat medium steam turbine generator 10 and the steam turbine generator 13 are used as constituent elements to generate electric power that is one form of power. By connecting with a compressor, a blower, a pump, a propeller, or the like, various forms of power may be taken out.

(5) In the third embodiment, the water vapor generator 3 in the second embodiment is replaced with the flash tank 17, but the water vapor generator 3 in the first embodiment may be replaced with the flash tank 17. .

(6) In the third embodiment, one flash tank 17 is provided. However, a plurality of flash tanks 17 are provided in parallel, and water R3 output from the water preheater 5 is provided in parallel by the plurality of flash tanks 17. May be steamed.

According to the present invention, the exhaust heat recovery method for acquiring effective energy by vaporizing water, and the effective energy than the exhaust heat recovery method for acquiring effective energy by vaporizing water and a liquid having a lower boiling point than the water. It is possible to provide an exhaust heat recovery system and an exhaust heat recovery method with high recovery efficiency.
Further, according to the present invention, as described above, since the effective energy recovery efficiency in the exhaust heat recovery is high, it is possible to provide an energy supply system that is higher in energy efficiency than in the past.

DESCRIPTION OF SYMBOLS 1 ... Exhaust gas pipe (heat conduction path), 2 ... High boiling-point heat-medium steam generator, 3 ... Steam generator, 4 ... High-boiling-point heat-medium preheater, 5 ... Water pre-heater, 6 ... High-boiling-point heat medium steam superheater 7 ... Steam superheater, 8 ... High boiling point heat medium supply pump, 9 ... Feed water pump, 10 ... High boiling point heat medium steam turbine generator, 11 ... High boiling point heat medium steam condenser (heat exchanger), 12 ... Recovery Liquid tank, 13 ... steam turbine generator, 14 ... steam condenser, 15 ... condensate tank, 16 ... cooling water supply device, 17 ... flash tank, 18 ... pressure pump, G ... high temperature exhaust gas, R1 ... high boiling point heat Medium, R2 ... high boiling point heat medium steam, R3 ... water, R4 ... water vapor, P1-P3 ... energy supply system, K1-K3 ... exhaust heat recovery unit (exhaust heat recovery system), W1 ... electric power generation unit, W2, W3 ... Power generation / steam output section

Claims (14)

A heat conduction path through which exhaust heat is conducted; and
An exhaust heat recovery system comprising a high boiling point heat medium steam generator that generates high boiling point heat medium steam by exchanging heat between a high boiling point heat medium having a higher evaporation temperature than water and exhaust heat conducted through a heat conduction path. The exhaust heat recovery system according to claim 1, further comprising a steam generator provided on the downstream side of the high-boiling-point heat medium steam generator in the heat conduction path and generating water vapor by exchanging heat with the exhaust heat. In the heat conduction path, on the upstream side of the high-boiling-point heat medium steam generator, the high-boiling-point heat medium steam superheater that superheats the high-boiling point heat medium steam by heat exchange with exhaust heat or superheats the steam by heat exchange with exhaust heat. The exhaust heat recovery system according to claim 1 or 2, comprising either or both of a steam superheater. The exhaust heat recovery system according to any one of claims 1 to 3, further comprising a high boiling point heat medium preheater for preheating the high boiling point heat medium and / or a water preheater for preheating water. The exhaust heat recovery system according to any one of claims 1 to 4, wherein the heat conduction path is an exhaust gas pipe through which exhaust gas having exhaust heat flows. The exhaust heat recovery system according to any one of claims 1 to 5, wherein the high boiling point heat medium is ethylene glycol, diethylene glycol, propylene glycol, propylene ethylene glycol, or formamide. The exhaust heat recovery system according to any one of claims 4 to 6, further comprising a flash-type steam generator that vaporizes water preheated by the water preheater by a flash phenomenon instead of the steam generator. The exhaust heat recovery system according to any one of claims 1 to 7,
While supplying the high boiling point heat medium or / and water to the exhaust heat recovery system, the high boiling point heat medium vapor or / and water vapor is recovered from the exhaust heat recovery system, and the high boiling point heat medium vapor or / and water vapor is used as the working fluid. An energy supply system comprising a power generation unit that generates power. The power generation unit includes a heat exchanger that heat-exchanges the high-boiling-point heat medium vapor and water after being used for generating power to condense and liquefy the high-boiling-point heat medium steam and generate water vapor. Energy supply system. An exhaust heat recovery method for recovering heat by evaporating a high boiling point heat medium having a higher evaporation temperature than water by exhaust heat. The exhaust heat recovery method according to claim 10, wherein water is vaporized by exhaust heat after heat recovery by a high boiling point heat medium to recover heat. The exhaust heat recovery method according to claim 10 or 11, wherein the high boiling point heat medium steam and / or steam is superheated by heat exchange with the exhaust heat. The exhaust heat recovery method according to any one of claims 10 to 12, wherein the high boiling point heat medium is ethylene glycol, diethylene glycol, propylene glycol, propylene ethylene glycol, or formamide. Instead of vaporizing water by exhaust heat after heat recovery with a high boiling point heat medium and recovering heat, water is preheated by exhaust heat after heat recovery with a high boiling point heat medium, and the preheated water is flushed The exhaust heat recovery method according to any one of claims 11 to 13, wherein the heat recovery is performed by evaporation.

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