Waste heat recovery system

Abstract: A waste heat recovery boiler comprising heat exchange rate switching means (34,35,36) for controlling the rate of heat exchange between an exhaust gas (G) and feedwater (WF) in a heat exchanger (5) by changing the state of the feedwater (WF) in accordance with the concentration of sulfur oxides in the exhaust gas (G), thereby maintaining the temperature at which low temperature corrosion due to the exhaust gas (G) is prevented in a downstream portion of the heat exchanger (5) in the direction in which the exhaust gas (G) flows. Accordingly, it is possible to achieve the maximum efficiency of heat recovery since the phenomenon of steaming in the heat exchanger (5) is eliminated irrespective of whether the kind of exhaust gas is a dirty gas or a clean gas.

Description: The present invention generally is related to waste heat recovery means for use in combined power plants, and more particularly, it is concerned with a waste heat recovery system of the kind defined in the preamble of the appended claim 1. Combined power plants have recently attracted attention as a highly efficient form of electric power generation. In such a combined power plant, the generation of electric power is performed by first generating electricity by means of a gas turbine, then recovering the heat inherent to the exhaust gases discharged from the gas turbine by means of a waste heat recovery heat exchanger, and then operating a steam turbine using the steam produced in the waste heat recovery heat exchanger. An exhaust gas heat recovery system as used hitherto in that kind of power plants is known from US-A-4 394 813. The said known system comprises an exhaust gas economizer having heat transfer sections including a preheating section, an evaporating section and a superheating section, a feed water heater, a steam separation drum, a low pressure steam generator and a mixed-pressure turbine and in operating the said system a temperature gradient of circulating water and a temperature gradient of exhaust gases are made substantially equal to each other in the preheating section of the exhaust gas economizer to prevent an exhaust gas economizer tube from being corroded by generated sulfuric acid. In that connection the temperature at the inlet of an economizer is controlled by controlling the mixing ratio at a heater so as to preventlow temperature corrosion from occurring. The said inlet temperature is controlled in accordance to the amount of SOx contained in the exhaust gas. The heat transfer area of the exhaust gas economizer is kept unchanged, and only the temperature is controlled depending on the amount of SOx present. Further, GB-A-2 099 558 discloses a combined cycle power plant in which otherwise wasted gas turbine exhaust gas is used to heat water into steam in a heat recovery steam generator which includes three heating sections, an economizer, an evaporator and a superheater. In operating the said heat recovery steam generator cooling water is fed into a middle portion of the economizer so as to prevent steaming from occurring at the outlet of the economizer. There is no controlling the temperature at the inlet of the economizer, and also the heat transfer area is kept unchanged. A typical example for a combined power plant of the prior art will now be explained below referring to a diagram of its overall system shown in Fig. 13 of the drawings. As illustrated, a fuel air A supplied through an air supply pipe 1 and a fuel F supplied through a fuel supply pipe 2 are mixed and burned in a combustor 3, and the resultant combustion gas causes the rotor of a gas turbine 4 to rotate, thereby generating electric power. After the combustion gas has been utilized in the gas turbine 4, the gas is introduced as an exhaust gas G into an exhaust gas passage 6 of a waste heat recovery boiler 5. A low pressure boiler 10 and a high pressure boiler 15 are arranged along the exhaust gas passage 6 from its downstream side to the upstream side. The low pressure boiler 10 includes a low pressure economizer 7, a low pressure evaporator 8 and a low pressure drum 9, and the high pressure boiler 15 includes a high pressure economizer 11, a high pressure evaporator 12, a high pressure drum 13 and a superheater 14. Feedwater WF which serves as a fluid to be heated is supplied by a feedwater pump 16 through a feedwater pipe 17 to the low pressure economizer 7. After being preheated to a predetermined temperature in the low pressure economizer 7, the feedwater WF is supplied through a drum feedwater pipe 18 to the low pressure drum 9. The feedwater WF supplied to the low pressure drum 9 is naturally or forcibly recycled through a low pressure descending pipe 19, the low pressure evaporator 8 and the low pressure drum 9. During this recycling, the feedwater WF is heated and separated into water and steam in the low pressure drum 9. The thus-separated water is further recycled through the low pressure descending pipe 19, the low pressure evaporator 8 and the low pressure drum 9, while the steam is supplied through a main steam pipe 20 to a steam turbine 21. In the meantime, high temperature water WR which is made to branch off at the outlet of the low pressure economizer 7 is partially supplied to the high pressure economizer 11 through a high pressure feedwater pipe 23 by means of a boiler feedwater pump 22. After being heated to a predetermined temperature in the high pressure economizer 11, the high temperature water WR is supplied through a drum feedwater pipe 24 to the high pressure drum 13. As with the low pressure boiler 10, the feedwater supplied to the high pressure drum 13 is recycled through a high pressure descending pipe 25, the high pressure evaporator 12 and the high pressure drum 13. During this recycling, the feedwater is separated into water and steam in the high pressure drum 13. The thus-separated steam is supplied through a drum steam outlet pipe 26 to the superheater 14. After the temperature of the steam is further raised in the superheater 14, it is supplied to the steam turbine 21 through a high pressure steam pipe 27. On the other hand, the water separated in the high pressure drum 13 is recycled through the high pressure descending pipe 25, the high pressure evaporator 12 and the high pressure drum 13. The liquid level of feedwater in each of the high pressure drum 13 and the low pressure drum 9 is controlled by operating a high pressure drum feed valve 28 and a low pressure drum feed valve 29, respectively. In Fig. 13, reference numeral 30 denotes a condenser, and reference numeral 31 denotes a generator. The steam which has been used for rotation of the rotor of the steam turbine 21 is changed into water in the condenser 30. The resultant water is again supplied as the feedwater WF through the feedwater pipe 17 to the waste heat recovery boiler 5 by means of the feedwater pump 16. However, the feedwater WF in the feedwater pipe 17 has a low temperature of about 34°C. Therefore, if the feedwater WF having such a low temperature is supplied to the low pressure economizer 7, low temperature corrosion will take place in the low pressure economizer 7. For this reason, it is necessary to raise the temperature of the feedwater to a predetermined temperature at which no low temperature corrosion occurs by mixing the feedwater WF with part of the high temperature water WR passing through the high pressure feedwater pipe 23. For this purpose, part of the high temperature water WR flowing in the high pressure feedwater pipe 23 is supplied from the outlet of the boiler feedwater pump 22 to the feedwater pipe 17 through a recycle channel 33 having a recycle flow regulating valve 32, thereby preventing the occurrence of low temperature corrosion within the low pressure economizer 7. It is to be noted that the waste heat recovery boiler 5 in the schematic system view of Fig. 13 is shown by way of example as employing as the fuel F a fuel, such as LNG, which exhausts a clean gas containing no sulfur. To cope with the recent trend toward diversification in the kinds of fuel employed, the waste heat recovery boiler 5 may of course employ as the fuel F a dirty oil fuel such as naphtha which contains sulfur. There are some instances where a waste heat recovery boiler which can be adapted to various kinds of fuel is planned and utilizes the aforesaid structure of the prior art waste heat recovery boiler 5. In such an instance, if the heat transfer area of the low pressure economizer 7 is designed on the assumption that a fuel is used which exhausts a gas containing no SOx (hereinafter referred to as a "clean gas"), it is necessary to raise the temperature of the feedwater at the inlet of the low pressure economizer 7 in order to prevent low temperature corrosion from occurring during the recovery of the heat possessed by the waste gas. This necessity involves the following shortcomings which will be described with reference to Figs. 14A and 14B. Figs. 14A and 14B are characteristic charts in which their horizontal axes uniformly represent the amount of SOx contained in the exhaust gas G, with the vertical axes of Figs. 14A and 14B representing the temperature of the exhaust gas at the outlet of the waste heat recovery boiler 5 and the temperature of the feedwater, respectively. In Figs. 14A and 14B, a common vertical line B which corresponds to a clean gas represents the fact that the amount of SOx is zero, while a common vertical line C which corresponds to a dirty gas represents the fact that the amount of SOx is 10 ppm. Curve D in Fig. 14A represents the temperature of the exhaust gas at the outlet of the low pressure economizer 7 when the heat transfer area of the low pressure economizer 7 is increased, with curve E in the same figure representing the temperature of the exhaust gas at the outlet of the low pressure economizer 7 when the heat transfer area of the low pressure econimizer 7 is reduced. In Fig. 14B, curve H represents the temperature of the feedwater at the inlet of the low pressure economizer 7, curve I representing the temperature of the feedwater at the outlet of the low pressure economizer 7 when the heat transfer area of the low pressure economizer 7 is increased, curve J representing the temperature of the feedwater at the outlet of the low pressure economizer 7 when the heat transfer area of the low pressure economizer 7 is reduced, curve K representing the steam generation temperature at which steam is generated in the low pressure economizer 7, and a shaded portion L representing the steam generation zone in which steam is generated in the low pressure economizer 7. As described previously, in order to prevent low temperature corrosion from occurring in the low pressure economizer 7 when either of a clean or dirty gas is exhausted, it is necessary to increase the flow rate of the high temperature water WR flowing in the recycle channel 33 shown in Fig. 13. However, when the flow rate of the high temperature water WR is increased, the temperature of the feedwater at the inlet of the low pressure economizer 7 rises along curve H from point M to point N. Accordingly, the temperature of the feedwater at the outlet of the low pressure economizer 7 rises from point O to point P as indicated by curve I, and the temperature within the low pressure economizer 7 reaches the steam generation zone indicated as the shaded portion L. This temperature increase results in the problem that the low pressure economizer 7 is damaged owing to the occurrence of adverse phenomena such as steaming, unstable flow, water hammer and so forth. In addition, the increase in the flow rate of the high temperature water WR involves the drawback of an increase in the capacity of the boiler feedwater pump 22. It is estimated that the pump capacity of the boiler feedwater pump 22 with respect to the dirty gas is about two times greater than that with respect to the clean gas. On the other hand, when the heat transfer area of the low pressure economizer 7 is reduced from curve I to curve J in order to prevent the phenomenon of steaming in the low pressure economizer 7, the temperature of the feedwater at the outlet of the low pressure economizer 7 falls from point P to point Q, thereby enabling prevention of the phenomenon of steaming. Since the temperature of exhaust gas at the outlet of the waste heat recovery boiler 5 rises from point R to point S, the occurrence of low temperature corrosion can also be prevented. However, when the clean gas is employed, the temperature of the exhaust gas at the outlet of the waste heat recovery boiler 5 rises from point T to point U in Fig. 14A, and thus in the water heat recovery boiler which is planned on condition that the clean gas is used, the temperature of the exhaust gas at its outlet is raised by about 15°C. Therefore, since a large quantity of heat to be recovered is dissipated in the atmosphere, the whole arrangement is uneconomical from the view point of heat recovery. Considering the prior art as outlined above, it is an object of the present invention to achieve a maximum efficiency of heat recovery while preventing both low temperature corrosion and the phenomenon of steaming from occurring, irrespective of the kind of the exhaust gas which may be a clean gas or a dirty gas containing SOx. The said object is achieved by designing a waste heat recovery system as indicated in the appended claim 1, a further development of the invention being defined in a subclaim. In a system according to the present invention the total of the heat transfer area of an economizer may be employed to enhance the efficiency of heat recovery when the exhaust gas used is a clean gas free from SOx. When the exhaust gas used is a dirty gas containing SOx, generally the temperature of the water fed to the inlet of the economizer should be high to prevent low temperature corrosion. Since, however, there is a risk that steaming might occur at the outlet of the economizer, there is another condition to be met which is contradictory to the said first condition. Therefore, according to the present invention to prevent both low temperature corrosion and steaming when using an exhaust gas which is a dirty gas containing SOx in combination reducing the heat transfer area of the economizer is employed. The said reduction of the heat transfer area is effected by changing the position for inputting and/or the position for outputting water to and from the economizer. In this manner, maximum heat recovery may be achieved while preventing both low temperature corrosion and steaming. The said combination offers a great technical advantage over the prior art in that it simultaneously achieves maximum efficiency of heat recovery, prevention of low temperature corrosion and prevention of steaming phenomena, irrespective of the nature of the exhaust gas which may be a clean gas or may be a dirty gas depending on the amount of SOx contained therein. The present invention will be more readily apparent from the following detailed description of a few preferred embodiments thereof when taken in conjunction with the accompanying drawings, in which: Fig. 1 is a system diagram illustrating the overall system of a combined power plant in accordance with the present invention; Fig. 2 is a system diagram illustration on an enlarged scale of the essential portion of the combined power plant shown in Fig. 1; Figures 3 to 12 are system diagrams of the invention. Fig. 13 is a system diagram illustrating the overall system of a typical example of a combined power plant which relies upon the prior art; Fig. 14A is a characteristic chart showing characteristic curves relative to the temperature of the exhaust gas at the outlet of a low pressure economizer; and Fig. 14B is a characteristic chart showing characteristic curves relative to the temperature of the feedwater in a low pressure economizer. The present invention will be described below with reference to the accompanying drawings. First of all, the present invention will be described in conjunction with Fig. 1 which is a system diagram illustrating the overall system of a combined power plant in accordance with the present invention, as well as Fig. 2 which is an enlarged system diagram of the essential portion of the combined power plant shown in Fig. 1. Throughout the figures which illustrate the present invention, reference numerals 1 to 31 denote the elements corresponding to those used in the waste heat recovery boiler of the prior art shown in Fig. 13. The invention further includes a first recycle flow regulating valve 34, a first recycle channel 35, a second recycle flow regulating valve 36, a second recycle channel 37, an inlet header 38 of the low pressure economizer 7, a middle header 39 of the same, an outlet header 40 of the same, a distributor 41, an SOx sensor 42 disposed in the exhaust gas passage 6 for sensing the concentration of SOx contained in the exhaust gas G, and a control section 43 for outputting a valve-opening command signal to the first recycle flow regulating valve 34 and the second recycle flow regulating valve 36 on the basis of a detection signal supplied from the SOx sensor 42, the control section 43 having a valve switching means 44 in its interior. An SOx reference value (for example, 0.1 ppm) is previously set in a storage portion (not shown) of the control section 43 in order to determining whether the kind of exhaust gas is a clean gas or a dirty gas. The control section 43 compares that reference value with the detected value supplied from the SOx sensor 42. If the detected value is less than the reference value, the control section 43 determines that the kind of exhaust gas is a clean gas, and supplies valve-opening command signals (to be described later) to the first and second recycle flow regulating valves 34 and 36. On the other hand, if the detected value is not less than the reference value, the control section 43 determines that the kind of exhaust gas is a dirty gas, and supplies to the same valves 34 and 36 valve-opening command signals which will be described later. By way of example, the system is arranged in such a manner that the SOx concentration in the exhaust gas is directly detected by the SOx sensor 42 to determine whether the kind of exhaust gas is a clean gas or a dirty gas. However, the SOx sensor 42 need not necessarily be incorporated. For example, if a gas fuel such as LNG which contains no sulfur is employed, the resultant exhaust gas is a clean gas, while, if an oil fuel such as naphtha which contains sulfur is employed, a dirty gas is produced. Therefore, suitable valve switching means may be disposed to supply valve-opening command signals to the recycle flow regulating valves 34 and 36 according to the kind of fuel employed. In Figs. 1 and 2, if the exhaust gas G is a clean gas, the second recycle flow regulating valve 36 is closed to stop the supply of the high temperature water WR to the second recycle channel 37. In the meantime, the first recycle flow regulating valve 34 is opened, and the high temperature water WR at the outlet of the boiler feedwater pump 22 is supplied to the first recycle channel 35, mixed with the feedwater WF in the feedwater pipe 17, and supplied to the inlet header 38 of the low pressure economizer 7. As more specifically shown in Fig. 2, the high temperature water WR in the first recycle channel 35 and the feedwater WF in the feedwater pipe 17 are made to flow through the inlet header 38 of the low pressure economizer 7 to the outlet header 40. Thus, all the heat transfer surfaces of the low pressure economizer 7 are employed to effect heat recovery of from point M to point O shown in Fig. 14B. On the other hand, if the exhaust gas G is a dirty gas, the first recycle flow regulating valve 34 is closed to stop the supply of the high temperature water WR to the first recycle channel 35. In the meantime, the second recycle flow regulating valve 36 is opened, and the high temperature water WR at the outlet of the boiler feedwater pump 22 is supplied to the second recycle channel 37, mixed with the feedwater WF in the feedwater pipe 17, and supplied to the middle header 39 of the low pressure economizer 7. As more specifically shown in Fig. 2, the high temperature water WR in the second recycle channel 37 and the feedwater WF in the feedwater pipe 17 are made to flow through the middle header 39 of the low pressure economizer 7 to the outlet header 40. Thus, the heat transfer surface of the low pressure economizer 7 is partially employed to reduce the heat transfer area thereof as compared with that used for the clean gas. If the heat transfer area of the low pressure economizer 7 is reduced in this manner, it is possible to effect heat recovery of from point N to point Q shown in Fig. 14B as well as to prevent steam from being produced in the low pressure economizer 7. It is to be noted that, in the case of the dirty gas, although no feedwater is supplied to the area defined between the inlet header 38 and the middle header 39 in the low pressure economizer 7, there is no problem from the strength viewpoint since the temperature of the exhaust gas G is sufficiently low. As described above, in order to solve the shortcomings involved in the prior art, the system is arranged so that, when the exhaust gas G is a clean gas, all the heat transfer surface of the low pressure economizer 7 is employed to enhance the efficiency of heat recovery. When the exhaust gas G is a dirty gas, the area of the heat transfer surface of the low pressure economizer 7 is reduced to prevent steaming from occurring in the low pressure economizer 7. Fig. 3 is a system diagram which differs to that shown in figures 1 and 2. In figure 1, the inlets of both the first recycle channel 35 and the second recycle channel 37 are made to branch from the outlet of the boiler feedwater pump 22, and the outlets of the channels 35 and 37 are respectively connected to the inlet header 38 and the middle header 39 of the low pressure economizer 7. In contrast, in figure 3, the inlet of the first recycle channel 35 is made to branch from the outlet of the boiler feedwater pump 22, while the inlet of the second recycle channel 37 is made to branch from the outlet of the higher pressure economizer 11. The outlets of the channels 35 and 37 are both connected to the inlet header 38 of the low pressure economizer 7. Accordingly, when the exhaust gas G is a clean gas, the first recycle flow regulating valve 34 is opened and the second recycle flow regulating valve 36 is closed, by a command signal from the switching means (not shown). Then, the high temperature water WR through the first recycle channel 35 and the feedwater WF through the feedwater pipe 17 are mixed and supplied to the low pressure economizer 7. On the other hand, if the exhaust gas G is a dirty gas, the first recycle flow regulating valve 34 is closed and the second recycle flow regulating valve 36 is opened. Then, the high temperature water WR through the second recycle channel 37 and the feedwater WF through the feedwater pipe 17 are mixed and supplied to the low pressure economizer 7. In other words, the system of figure 3 is arranged in such a manner that a position at which the high temperature water WR is extracted is switched between the outlet of the high pressure economizer 11 and the outlet of the low pressure economizer 7 in order to limit an increase in the flow rate of the high temperature water WR. More specifically, when the exhaust gas G is a clean gas, the high temperature water WR at the outlet of the low pressure economizer 7 is recycled to the first recycle channel 35, since the temperature of the feedwater at the inlet of the low pressure economizer 7 may be low. On the other hand, when the exhaust gas G is a dirty gas which requires that the temperature of the feedwater at the inlet of the low pressure economizer 7 be made high, the high temperature water WR at the outlet of the high pressure economizer 11 which is higher in temperature than that at the outlet of the low pressure economizer 7 is recycled through the second recycle channel 37. Thus, in the case of the dirty gas, since the temperature of the high temperature water WR is high, it is possible to limit an increase in the recycle flow in the second recycle channel 37 and hence to reduce the capacity of the boiler feedwater pump 22. Fig. 4 is a system diagram which differs from the aforesaid figure 3 in that the high temperature water WR is extracted at the distributor 41 of the high pressure descending pipe 25, and supplied to the second recycle channel 37. In the system of figure 4, when the exhaust gas G is a clean gas, the high temperature water WR at the outlet of the boiler feedwater pump 22 is supplied to the low pressure economizer 7 through the first recycle channel 35. On the other hand, when the exhaust gas G is a dirty gas, still higher temperature water WR is supplied from the distributor 41 through the second recycle channel 37 to the low pressure economizer 7, thereby preventing steaming and low temperature corrosion from occurring in the low pressure economizer 7. In addition, since the high temperature water WR may be supplied through the second recycle channel 37 at a reduced flow rate, it is possible to reduce the capacity of the boiler feedwater pump 22. Fig. 5 is a system diagram which differs from figures 1 to 4 in the following respect. In figures 1 to 4, the first recycle channel 35 and the second recycle channel 37 are disposed in parallel on the inlet side of the low pressure economizer 7 so that the heat transfer area may be changed. In contrast, in figure 5, a first extraction channel 46 having a first extraction flow regulating valve 45 is connected to a final outlet header 40a of the low pressure economizer 7, while a second extraction channel 48 having a second extraction flow regulating valve 47 is connected to a middle header 40b of the low pressure economizer 7 on the outlet side thereof. As illustrated, the other ends of these extraction channels 46 and 48 are connected to the drum feedwater pipe 18. Therefore, when the exhaust gas G is a clean gas, the second extraction flow regulating valve 47 is closed to stop the extraction of the feedwater in the second extraction channel 48. Then, the first extraction flow regulating valve 45 is opened to extract the feedwater from the final outlet header 40a. On the other hand, when the exhaust gas G is a dirty gas, the first extraction flow regulating valve 45 is closed to stop the extraction of the feedwater in the first extraction channel 48. Then, the second extraction flow regulating valve 47 is opened to extract the feedwater from the middle outlet header 40b. In this manner, the heat transfer area of the low pressure economizer 7 can be changed, depending upon whether the exhaust gas G is a clean gas or a dirty gas. Thus, it is possible to prevent steaming and low temperature corrosion from occurring in the low pressure economizer 7, as well as to recover the heat possessed by the exhaust gas G at the maximum efficiency. It is to be noted that, in the case of a dirty gas, no feedwater flows in the area defined between the middle outlet header 40b of the low pressure economizer 7 and the final outlet header 40a thereof. However, there is no risk of damaging the heat transfer surface of the economizer 7 since the gas temperature on the inlet side of the low pressure economizer 7 is low. Fig. 6 is a system diagram which differs from the previously-described figures 1 and 2 in that a main recycle channel 50 having a flow regulating valve 49 extends from the outlet side of the boiler feedwater pump 22 to the feedwater pipe 17. The downstream end of the main recycle channel 50 is provided with an inlet header feedwater pipe 53 having a first stop valve 51 and a middle header feedwater pipe 54 having a second stop valve 52. As illustrated, the inlet header feedwater pipe 53 is connected to the inlet header of the low pressure economizer 7, and the middle header feedwater pipe 54 is connected to the middle header of the low pressure economizer 7. When the exhaust gas G is a clean gas, the first stop valve 51 is opened and the second stop valve 52 is closed, and the high temperature water WR supplied through the main recycle channel 50 is mixed with the feedwater WF. The mixed flow is supplied through the inlet header feedwater pipe 53. When the exhaust gas G is a dirty gas, the first stop valve 51 is closed and the second stop valve 52 is opened, and the high temperature water WR supplied through the main recycle channel 50 is mixed with the feedwater WF. The mixed flow is supplied through the middle header feedwater pipe 54. Fig. 7 is a system diagram which differs from figure 3 in that, as in figure 6, the inlet header feedwater pipe 53 having the first stop valve 51 and the middle header feedwater pipe 54 having the second stop valve 52 are incorporated. With this arrangement, it is possible to provide further fine control over the low pressure economizer 7 by effecting suitable switchover between the two flow regulating valves 34 and 36 as well as the two stop valves 51 and 52. More specifically, the following control is enabled according to the nature of the exhaust gas G. (1) The first recycle flow regulating valve 34 is opened and the second recycle flow regulating valve 36 is closed so as to control the opening and closing of the first stop valve 51 and the second stop valve 52. (2) The first recycle flow regulating valve 34 is closed and the second recycle flow regulating valve 36 is opened so as to control the opening and closing of the first stop valve 51 and the second stop valve 52. (3) The first stop valve 51 is opened and the second stop valve 52 is closed so as to control the opening and closing of the first recycle flow regulating valve 34 and the second recycle flow regulating valve 36. (4) The first stop valve 51 is closed and the second stop valve 52 is opened so as to control the opening and closing of the first recycle flow regulating valve 34 and the second recycle flow regulating valve 36. Fig. 8 is a system diagram which differs from the previously-described figure 5 in that, although the boiler of figure 5 has a single pressure stage, that of figure 8 has a plurality of pressure stages. More specifically, the boiler feedwater pump 22 and the high pressure feedwater pipe 23 are incorporated, and the high temperature water WR is partially supplied through the recycle channel 35, and is mixed with the feedwater WF. Fig. 9 is a system diagram which differs from the above-described figure 7 in that the recycle line extending from the outlet of the boiler feedwater pump 22 is omitted, whereby the high temperature water WR is partially recycled through the outlet of the high pressure economizer 11. Fig. 10 is a system diagram which differs from the above-described figure 9 in that the high temperature water WR is partially recycled via the distributor 41 of the high pressure descending pipe 25. Fig. 11 is a system diagram which differs from the above-described figure 9 in that a high temperature fluid (a mixture of steam and the high temperature water WR) is partially recycled through the outlet of the high pressure evaporator 12. Fig. 12 is a system diagram which differs from the above-described figure 9 in that high pressure steam is partially recycled through the outlet of the high pressure steam pipe 27. In the systems showns in figures 9 to 12 in which a fluid having a still higher temperature is recycled, the flow rate of recycled fluid can be reduced. Although some of the above-described systems have two recycle lines, two or more recycle lines may of course be provided. Also, some of the above-described systems have two positions at which the feedwater is supplied or extracted. However, more than two feedwater supply positions and/or feedwater extracting positions may be provided. Further, by way of example, the economizer of the low pressure boiler has specifically been described in the explanation of the respective figures. However, it is of course possible to control other heat exhangers in a similar manner to that described above. The present invention provides the following advantages. (1) The heat transfer area of the heat exchanger can be adjusted by changing the position at which the feedwater is supplied to or extracted from the heat exchanger in correspondence with the kind of fuel employed. Accordingly, the maximum efficiency of heat recovery can be achieved for each kind of fuel. It is estimated that heat recovery is improved by about 5% as compared with the prior art waste recovery boiler, so that annual fuel costs can be reduced by 1.5 billion yen per four boilers. (This estimation is based on the condition that a 1,000-MW plant (including four waste heat recovery boilers) operates for an operating time of 6,000 hours/year at a plant efficiency of 40% with a fuel cost of 7 yen/1,000 kcal.) (2) In addition, it is possible to limit the increase in capacity of the boiler feedwater pump irrespective of the presence or absence of SOx in the exhaust gas. (Examples of Estimations) 1. If the fuel for the gas turbine is LNG (containing no SOx in its exhaust gas), the shaft power of the boiler feedwater pump is 600 KW. 2. If the fuel for the gas turbine is naphtha (containing SOx in its exhaust gas), (1) when the high temperature water WR is extracted through the outlet of the low pressure economizer, the shaft power of the boiler feedwater pump is 1,200 KW; and (2) when the high temperature water WR is extracted through the outlet of the high pressure economizer, the shaft power of the boiler feedwater pump is 610 KW. Therefore, in accordance with the present invention, it is possible to reduce the shaft power of the boiler feedwater pump to substantially half the normal level and hence to reduce the operating cost of the plant. Accordingly, in accordance with the present invention, whether the kind of exhaust gas is a clean gas or a dirty gas, the heat recovery of the exhaust gas can be accomplished at its maximum efficiency by eliminating the phenomenon of steaming and low temperature corrosion in the heat exchanger.

Claims: A waste heat recovery system, comprising a heat exchanger (5) which is fed with an exhaust gas (G) and with feedwater (WF) to be used for generating steam for feeding a steam turbine (21) and control means for controlling the rate of the heat exchange between said exhaust gas and said feedwater in said heat exchanger so as to maintain the temperature in said heat exchanger above the value at which low temperature corrosion may occur, characterised in that said control means include first changing means (45, 47; 51, 52) changing the heat transfer area of said heat exchanger (5) by changing the position (38, 39) at which said feedwater (WF) is supplied to said heat exchanger (5) and/or changing the position (40a, 40b) at which said feedwater (WF) is extracted from said heat exchanger (5) and/or second changing means (34; 36; 49) changing the temperature of said feedwater (WF) to be supplied to said heat exchanger (5) by means of a plurality of high temperature fluid mixing lines (35, 37; 50) which are switchable to supply fluid at different high temperatures for mixing part of a high temperature fluid heated in said heat exchanger (5) with said feedwater (WF), said first and second changing means being operable independently of each other. A system according to claim 1, charaterised in that it further includes sensor means (42) for detecting the concentration of sulphur oxides in said exhaust gas (G) circulating through said heat exchanger (5) and that said control means includes switching means (44) arranged to actuate said changing means (34, 36; 45, 47; 49; 51, 52) in response to a detection signal from said sensor means (42).

Inventors: KUSAKA IWAO, SHIGENAKA TOSHINORI, KUSAKA, IWAO, SHIGENAKA, TOSHINORI
Applicants: BABCOCK HITACHI KK, BABCOCK-HITACHI KABUSHIKI KAISHA
Application year: 1988
Main classification: F22B1
IPC codes: F22B1, F01K23