JP2009133318A - System having compressor equipped with multiple middle coolers, and cooling method - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide a middle cooling device having a structure capable of cooling cooled gas to saturation temperature without controlling a water injection amount, and capable of suppressing the deterioration of the reliability of a compressor and improving efficiency, for solving a problem wherein the actual temperature of compressed gas at an outlet of a middle cooler is higher than the saturation temperature even if controlling the water injection amount so as to cool the compressed gas to the saturation temperature, because a margin needs to be set when controlling the water injection amount in the middle cooler and the accuracy of properly adjusting the water injection amount by controlling has limits. <P>SOLUTION: The middle cooling mechanism of this invention is installed between stages of a gas compressor constituted by multiple compressing stages, and cools the compressed gas of the compressor. The compressed gas is cooled by spraying liquid of not less than required amount, and a means for suppressing the inflow of the liquid into the compressing stages is provided. <P>COPYRIGHT: (C)2009,JPO&INPIT

Description

  The present invention relates to a system such as a gas turbine system or a heat pump system using a cooling device for a fluid to be compressed of a gas compressor that compresses air, water vapor, or the like, and a method for cooling a working medium.

As an intermediate cooling of a gas compressor that compresses air or water vapor, a method of cooling a compressed gas of the compressor by spraying water is known. For example, JP 2005-274070 discloses a method for cooling a high-temperature fluid such as a gas to be compressed during a compression process in a compressor. An apparatus is disclosed.

In the method of cooling the compressed gas to near the saturation temperature by water injection in the intermediate cooler of the compressor, it is necessary to suppress the erosion due to excessive water injection and the decrease in cooling efficiency due to under water injection. Therefore, conventionally, when the gas to be compressed is cooled to near the saturation temperature by water injection into the intermediate cooler, it is essential to control the water injection amount based on the steam temperature on the outlet side of the intermediate cooler.

JP 2005-274070 A

  When controlling the amount of sprayed water with an intercooler that sprays water, it is necessary to consider the measurement error of the measurement value that serves as the control reference, and the time difference from the measurement until the adjustment of the sprayed water amount is completed. . Since it is necessary to set a margin that takes these into account, there is a limit to the accuracy with which the amount of water injection is appropriately adjusted by control. Therefore, even if the amount of water injection is controlled to cool the compressed gas to the saturation temperature, the temperature of the compressed gas at the outlet of the intermediate cooler is actually higher than the saturation temperature, and the efficiency of the compressor is low by this amount. . The objective of this invention is providing the cooling device which can achieve the efficiency improvement of a compressor.

  In order to achieve the above object, a system of the present invention includes a first compressor that compresses a working fluid and a first compressor that cools the working fluid compressed by the first compressor by direct contact heat exchange with water. An intermediate cooler, a second compressor that compresses the working medium cooled by the first intercooler, and the working medium compressed by the second compressor by direct contact heat exchange with water. A system comprising: a second intercooler for cooling; and a third compressor for compressing the working medium cooled by the second intercooler, wherein water is supplied to the first intercooler. A supply system; and a system for supplying water from the first intermediate cooler to the second intermediate cooler.

  ADVANTAGE OF THE INVENTION According to this invention, the cooling device which can achieve the efficiency improvement of a compressor can be provided.

1 shows a simple cycle gas turbine system to which an intermediate cooling mechanism that is Embodiment 1 of the present invention is applied. The detailed drawing of the cooling tower 36 of Example 1 of this invention is shown. 1 shows a regeneration cycle gas turbine system including an intermediate cooling mechanism for a compressor that is Embodiment 1 of the present invention. 6 shows a regeneration cycle gas turbine system including an intermediate cooling mechanism for a compressor that is Embodiment 2 of the present invention. The graph which each represents the distribution of the temperature with respect to the height direction position in the packing 71 installation part inside the cooling tower 36 of Example 1 of this invention, an absolute humidity, and humidification amount is shown. The graph showing the distribution of the temperature, the absolute humidity, and the humidification amount with respect to the height direction position in the packing 71 installation part inside the cooling tower 36 of Example 2 of the present invention is shown. A detailed view of the cooling tower 36 of the present invention is shown. A detailed view of the cooling tower 36 of the present invention is shown. The steam heat pump system provided with the intermediate cooling mechanism of the compressor which is Example 3 of this invention is shown. The graph which each represents temperature, the flow volume, and the distribution of a vapor pressure with respect to the height direction position in the packing 71 installation part inside the cooling tower 36 of Example 3 of this invention is shown. The transition of temperature, pressure, and mass flow rate when the cooling tower of Example 3 of the present invention is operated and when not operated is shown.

  A technique for improving the compression efficiency of the compressor will be described. In the gas compressor, the density of the gas to be compressed is increased by intercooling the gas to be compressed, the power required for the compression is reduced, and the compression efficiency is improved. Also, water is sprayed on the compressed gas sucked into the compressor to cool the compressed gas, and the sprayed power is evaporated by evaporating the sprayed water due to the heat of the compressed gas and the temperature rise effect in the compressor. The flow rate of the compressed gas, which is the main fluid of the compressor, is increased while reducing the pressure.

  When water is sprinkled into the compressed gas in the intermediate cooling device of the compressor, the flow rate of the compressed gas can be increased while reducing the compression power of the compressor. Increasing the flow rate of the compressed gas in the intercooler means that more gas can be compressed with the same compression power, which leads to further improvement in compression efficiency.

  As described above, when water is sprayed in the intercooler of the compressor, the compression efficiency of the compressor is improved by two effects of the cooling effect of the compressed gas and the increase effect of the compressed gas by evaporation of the sprayed water. . At this time, the compression efficiency becomes maximum when the gas to be compressed is cooled to the saturation temperature. Therefore, in order to improve the compression efficiency, it is desirable to spray a large amount of water that can cool the compressed gas to the saturation temperature.

  However, if the amount of sprayed water in the intercooler is too large, the sprayed water that could not evaporate in the intercooler flows into the compressor and the droplets collide with the compression stage that rotates at high speed, causing a mechanical condition called erosion. Erosion occurs, reducing the reliability of the compressor.

  In order to improve the compression efficiency as much as possible without reducing the reliability of the compressor, the amount of sprayed water should be set so that as much water as possible can be sprayed without exceeding the amount of water that can be evaporated in the intercooler. It is desirable to control.

  As an appropriate method for determining the amount of sprayed water, for example, it is conceivable to use the compressed gas temperature at the outlet of the intercooler as a reference. The pressure of the compressor mainstream is a substantially constant value determined by design, and if the pressure is constant, the saturation temperature at that pressure is also uniquely determined. If the temperature of the compressed gas at the outlet of the intermediate cooler is set to be about 5 ° C. to 10 ° C. higher than the saturation temperature, the compressed gas at the outlet of the intermediate cooler is in an overheated state, and the sprayed water does not evaporate. There is little possibility to flow into the compressor in the state.

  In this example, setting the temperature of the compressed gas to be about 5 ° C to 10 ° C higher than the saturation temperature without setting it as the saturation temperature, the measurement error of the gas temperature, and the adjustment of the water injection amount after measurement are completed This is because it is necessary to take a margin in consideration of the time difference until it is done. This margin needs to be set so that the temperature of the compressed gas becomes high. If the compressed gas temperature at the outlet of the intercooler becomes lower than the saturation temperature, the compressed gas here is in a saturated state. Sex declines.

  A technique based on measurement values other than the intermediate cooler outlet temperature is also conceivable. However, in order not to reduce the reliability of the compressor, it is necessary to set a margin, and the margin is set so that the temperature of the compressed gas becomes high. That is, it is difficult to cool the compressed gas to the saturation temperature by the method of controlling the amount of sprayed water.

  In the above-described method for controlling the amount of sprayed water, it is assumed that all of the water sprayed in the intercooler evaporates unless the compressed gas is saturated. In the intercooler in which this precondition is not satisfied, since the amount of water remaining without being evaporated is large, the margin must be set more, and the cooling effect of the compressed gas is low.

  In order to efficiently exchange heat between the compressed gas and the spray water so as to satisfy this precondition, it is desirable to increase the contact area between the compressed gas and the spray water. To this end, it is conceivable to lengthen the gas-liquid contact flow path in the intermediate cooling device and to make the size of the droplets of the sprayed water fine. The equipment cost becomes higher.

  On the other hand, the intermediate cooling device according to the embodiment of the present invention is not based on the control of the amount of sprayed water, but is structurally configured to cool the compressed gas to the saturation temperature while suppressing a decrease in the reliability of the compressor. Yes.

  Specifically, it has means for suppressing the inflow of sprayed water into the compressor, and the compressed gas is configured to be cooled by a desired amount or more of sprayed water. Here, the desired amount means an amount of water that can cool the temperature of the compressed gas at the outlet of the intermediate cooling device to the saturation temperature.

As a means for suppressing the inflow of sprayed water to the compressor, for example, a flow path is configured to flow the compressed gas from below to above in the intercooler, and between the inlet and outlet of the compressed gas. There is a method of installing a water spray device and installing a mist remover, which is a liquid passage suppression device, between the water spray device and the compressed gas outlet. With such a configuration, most of the water that is not evaporated and remains in a liquid state flows down due to the action of gravity and is unlikely to flow into the compressor from the compressed gas outlet. It is conceivable that some fine droplets flow upward in the flow path along the flow of the compressed gas, but these fine droplets are caught by the mist remover installed just before the flow path outlet. Therefore, since the inflow into the compressor is suppressed, a decrease in reliability can be suppressed.
By comprising in this way, to-be-compressed gas can be cooled to saturation temperature, without reducing the reliability of a compressor. In other words, if the intermediate cooling device according to the embodiment of the present invention is used, the compressed air can be further cooled by an amount that does not require a margin setting as compared with the control of the amount of sprayed water, and the compression efficiency can be further improved. is there. This is a configuration in which the use of gravity and the installation of a mist remover suppresses the inflow of liquid water into the compressor and then sprays more water than the desired amount, thereby suppressing the reduction in compressor reliability and being compressed. This is because the cooling to the gas saturation temperature can be achieved in principle.

  Hereinafter, the cooling device of the present invention will be described in detail using examples.

  The embodiment of the present invention will be described in detail with reference to FIG. FIG. 3 shows a regeneration cycle gas turbine system including an intermediate cooling mechanism for a compressor according to an embodiment of the present invention.

  The main components of the regenerative cycle gas turbine system of this embodiment are compressors 10a and 10b that compress air, and a regenerative heat exchanger that heats the compressed air obtained by compression by the compressor 10b with the exhaust gas of the gas turbine. 60, a combustor 12 that burns air heated by the regenerative heat exchanger 60 and the fuel 50 to generate combustion gas, a turbine 14 that is driven by the combustion gas generated by the combustor 12, and a turbine 14 Is a stack 82 in which the combustion gas heat-exchanged with the compressed air by the regenerative heat exchanger 60 is discharged as exhaust gas. In this embodiment, it is assumed that the pressure ratio of the gas turbine is 16, the pressure ratios of the compressors 10a and 10b are 4, and the intake flow rate of the gas turbine is 10 kg / s. The temperature efficiency of the regenerative heat exchanger was assumed to be 90%, and the polytropic efficiency of the compressor and turbine was assumed to be 90% and 88%, respectively. The power obtained from the output shaft of the gas turbine is converted into electric power by the generator 16 and connected to the power transmission system.

  A characteristic component in the present embodiment is a cooling tower 36 which is an intermediate cooling mechanism installed in the discharge pipe 86a of the compressor 10a. The cooling tower 36 will be described in detail with reference to FIG.

  FIG. 2 shows a detailed view of the cooling tower 36. The cooling tower 36a shown in FIG. 2 is provided with a circulation pump 6 that recirculates the circulating water dropped to the lower part of the tower above the packing 71 in the tower. The liquid reservoir 74 can be supplied with makeup water by the water supply pump 7 and the regulating valve 38. The gas distributor 70 serving as an inlet for the compressed air is installed to disperse the compressed air led from the compressor 10a through the discharge pipe 86a so as not to concentrate on a certain part in the cooling tower 36a. The gas disperser 70 has an opening downward to avoid inflow of liquid droplets falling from above. The cooling tower 36 shown in FIG. 2 is a packed tower using a packed material 71. The filling 71 is installed above the gas distributor 70 in order to widen the effective area of gas-liquid contact. As the filling 71, for example, a structure having a large surface area per volume generally used in a chemical plant or the like is used. In this embodiment, a commercially available irregular filling is used as the filling 71. As the tower diameter of the cooling tower 36a, a tower diameter of 1.8 m was applied because of the flooding characteristics generally disclosed as the performance specifications of the packing 71. Flooding is a packed tower or perforated plate tower that flows down a liquid film opposite to an upward gas flow. When the gas flow rate increases, the sprayed water is directed downward by the upward force received from the gas flow. It is a phenomenon that can no longer flow. The packing height of the packing material 71 is 0.8 m, assuming that the air temperature at the outlet of the cooling tower 36 a is around 60 ° C. when water of about 35 ° C. is sprayed. A mist remover 72, which is a fluid passage restraint device that restrains the inflow of liquid to the compressor, is a liquid such as entrainment generated by the shearing force between the upward air flow and the downward liquid film flow on the surface of the filling 71. The droplets are removed, and the inflow of the droplets to the downstream compressor 10b is suppressed. Therefore, it is desirable to install the mist remover 72 above the filler 71 and the liquid distributor 80. The circulation pump 6 sucks liquid phase water from a liquid pool 74 below the cooling tower 36 a through a pipe 76.

  In this embodiment, the water discharged from the circulation pump 6 is heat-exchanged with the low-temperature cooling water 91 by the heat exchanger 90. The circulating water cooled by the heat exchanger 90 is adjusted in flow rate by the regulating valve 84 and supplied to the cooling tower 36a from the liquid disperser 80 installed above the packing. The liquid disperser 80 is generally used in a chemical plant or the like, and has a function of spraying liquid phase water over the entire surface of the packing as evenly as possible. A water level gauge 78 is installed in the cooling tower 36a to control the water level of the liquid reservoir 74 to a desired position. When the water level of the liquid reservoir 74 decreases, the adjustment valve 38 of the pipe 75 is operated. Supply makeup water from the water source. When the water level of the liquid pool 74 rises, the adjustment valve 39 of the pipe 79 is operated to discharge the liquid phase water out of the system.

  Next, the operation | movement at the time of the steady state of the regenerative cycle gas turbine power generation system provided with the intermediate cooling mechanism of a present Example is demonstrated using FIG.

  Air sucked into an unillustrated intake chamber is compressed to about 400 kPa by the compressor 10a after dust and the like are removed by an unillustrated intake filter. The compressed air flows into the cooling tower 36. In the cooling tower 36, the water having a mass flow rate of about 35 ° C., which is cooled by the heat exchanger 90, is sprayed on the surface of the packing 71. In the case of atmospheric conditions with an air temperature of 15 ° C. and a relative humidity of 60%, the dew point temperature of the compressed air at the inlet of the cooling tower 36 is about 29 ° C., and the air is humidified by coming into gas-liquid contact with water higher than the dew point temperature. While being cooled.

  FIG. 5 is a graph showing the distribution of temperature, absolute humidity, and humidification amount with respect to the height direction position in the packing 71 installation portion inside the cooling tower 36 in this embodiment, and (a) shows the temperature. (B) shows the absolute humidity, and (c) shows the humidification amount. As shown in FIG. 5A, about 174 ° C. air (solid line) flowing from the lower side of the cooling tower 36 exchanges heat with about 35 ° C. liquid film (broken line) flowing down the surface of the packing 71 from above. However, the temperature becomes lower as it flows upward. The gas-liquid interface between the liquid film and air is covered with moist air having a saturated water vapor pressure corresponding to the temperature of the liquid film. As shown in FIG. 5B, in the lower region of the packing 71, the absolute humidity of the humid air (broken line) on the surface of the liquid film is higher than the absolute humidity (solid line) of the mainstream humid air. As shown in FIG. 5C, water vapor moves from the liquid film surface into the mainstream air. As a result, the absolute humidity of the mainstream air increases as it flows upward. However, since the liquid film water temperature is low in the upper region of the filling 71, this relationship is reversed, the absolute humidity in the mainstream air is increased, and moisture in the mainstream air is condensed and moved to the liquid film. When the low temperature water of about 35 ° C. was brought into contact with the compressed air of about 174 ° C. as in this example, the humidification amount from the low temperature water to the air was relatively small and about 0.6% by mass of the air mass. . On the other hand, the air temperature at the outlet of the cooling tower is cooled to about 62 ° C. That is, the mainstream air is cooled by the cooling tower 36 at 100 ° C. or more. The liquid film water dropped from the filling 71 flows down to the liquid pool 74 of the cooling tower 36. Moisture lost due to evaporation is supplied to the liquid reservoir 74 via the water supply pump 7 and the regulating valve 38. The heat exchanger 90 is supplied with hot water at about 55 ° C. from the liquid reservoir 74 by the circulation pump 6. In the heat exchanger 90, the hot water at about 55 ° C. is cooled to about 35 ° C. by heat exchange with the low-temperature cooling water 91 and is supplied to the cooling tower 36 again.

  The compressed air cooled to about 62 ° C. by the cooling tower 36 is sucked into the compressor 10b from the suction pipe 85b and compressed to 1600 kPa. The temperature at this time is about 240 ° C. In this embodiment, since the intake air temperature of the compressor 10b is relatively low at approximately 62 ° C. and the discharge temperature is approximately 240 ° C., the compression power can be significantly reduced as compared with the case where these temperatures are high.

  Table 1 shows a case where an intermediate cooling mechanism is provided and not provided in a virtual compressor having a pressure ratio of 16 in which two compressors having a pressure ratio of 4 shown in this embodiment are connected in series. The table which compared the compression power of was shown. It can be seen that when the mainstream air is cooled to about 62 ° C. by the intermediate cooling mechanism, the compression power can be reduced by about 17%.

  The compressed air of about 240 ° C. in the discharge pipe 86b flows into the heated fluid flow path of the regenerative heat exchanger 60, exchanges heat with the exhaust gas of the turbine 14 of about 560 ° C., and is heated to about 530 ° C. This compressed air is supplied from the heated fluid outlet pipe 61 of the regenerative heat exchanger 60 to the combustor 12 and combusted together with the fuel 50 to become a combustion gas of about 1300 ° C. Since the compressed air supplied to the combustor 12 is heated by the regenerative heat exchanger 60, the flow rate of the fuel 50 required at this time can be saved significantly compared to the case without the regenerative heat exchanger 60, and the plant thermal efficiency is improved. To do. The high-temperature combustion gas is supplied to the turbine 14 and passes through a stationary blade and a moving blade (not shown), whereby thermal energy is converted into rotational kinetic energy through an expansion process. The rotational kinetic energy drives the generator 16 connected to the same shaft, and is extracted as electric energy. The combustion exhaust gas of about 560 ° C. discharged from the turbine 14 through the expansion process is supplied to the exhaust gas flow path of the regenerative heat exchanger 60 and used for heating the compressed air as described above. Further, the combustion exhaust gas at about 340 ° C. discharged from the regenerative heat exchanger 60 is guided to the stack 82 and released into the atmosphere.

  In the present embodiment, the liquid water before being sprayed in the cooling tower 36 is cooled by the heat exchanger 90. By setting it as such a structure, the cooling efficiency of the mainstream air in a cooling tower can be improved. Since the heat exchanger 90 performs heat exchange between liquid and liquid, the overall heat transfer coefficient is larger than that of a heat exchanger that performs heat exchange between gas and liquid, and there is an advantage that the heat exchanger 90 can be configured compactly. Furthermore, the temperature of the water flowing through the heat exchanger 90 is about 55 ° C. at the maximum, and high corrosion resistance is not required. Therefore, a relatively inexpensive one such as a plate type can be used as the heat exchanger 90.

  In this embodiment, the liquid water in the liquid reservoir 74 is also circulated by the pump 6 and used as spray water from the liquid disperser 80. Of the sprayed water, the water that has not evaporated even after heat exchange with the mainstream air flows down to the liquid reservoir 74. Thus, by using a configuration in which a part of the liquid water sprayed for cooling the mainstream air can be sprayed again, the water can be effectively used and the amount of water supplied from the outside can be reduced.

  The pressure vessel, packing 71 and the like of the cooling tower 36 are mass-produced products generally used in chemical plants and are relatively inexpensive. Further, of the circulating water circulating from the cooling tower 36 via the heat exchanger 90, it is a part of the liquid film surface that evaporates, and the impurities are concentrated in the circulating water. In addition, in order to suppress the deterioration of the water quality of the liquid pool 74 due to the concentration of impurities contained in the makeup water, the regulating valve 39 is operated to discharge part of the liquid phase water out of the system continuously or intermittently. It is desirable to do.

  FIG. 1 shows a simple cycle gas turbine to which the intermediate cooling mechanism of this embodiment is applied. Up to this point, the example in which the intermediate cooling mechanism is applied to the regenerative cycle gas turbine has been described with reference to FIG. 3, but as shown in FIG. 1, the intermediate cooling mechanism of the present embodiment is applied to the simple cycle gas turbine. You may apply. An advantage of applying the intermediate cooling mechanism to the simple cycle or the regeneration cycle is that the compression power can be reduced as described above. In addition, cooling the compressed air has the effect of avoiding a high temperature of the members of the compressor and extending the life. In addition, when using the bleed air from a compressor for cooling a turbine high temperature member, the temperature of the cooling air used for cooling a turbine member can be lowered | hung by carrying out intermediate cooling of a compressor, and it can save the amount of cooling air .

  With respect to the regenerative cycle gas turbine, the discharge temperature of the compressor 10b is also lowered by the intermediate cooling action, so that an effect of increasing the amount of exhaust heat recovered that can be recovered from the exhaust gas by the regenerative heat exchanger 60 is also obtained. That is, in terms of power generation efficiency, a higher effect can be obtained when the intermediate cooling mechanism of the present embodiment is applied to the regeneration cycle gas turbine shown in FIG. 3 than when it is applied to a simple cycle gas turbine.

  FIG. 7 shows a detailed view of the cooling tower 36. The cooling tower 36b shown in FIG. 7 is a perforated plate tower using a perforated plate 92 instead of the packing 71 in the cooling tower 36a shown in FIG. When the perforated plate 92 is used for the cooling tower 36, the gas and liquid in the tower have a good geometric flow rate distribution and are more resistant to dirt than the packed tower. The advantage of the packed column compared with the perforated plate column is that the contact efficiency per volume is high and the pressure loss is small.

  FIG. 8 shows a detailed view of the cooling tower 36. The cooling tower 36c shown in FIG. 8 is a spray tower configured to spray a large amount of droplets from the spray nozzle 93 instead of installing the packing 71 in the cooling tower 36a shown in FIG. The spray tower has an advantage that the pressure loss on the gas side is smaller than that of the packed tower or the perforated plate tower.

  Particularly in a spray tower in which heat exchange between droplets and mainstream air is performed in a space, it is desirable to spray droplets having a predetermined size or more. The predetermined size means that the water does not completely evaporate with respect to one droplet, and the droplets do not evaporate and do not evaporate and remain in the liquid pool 74.

  Here, for example, in the case where a fine droplet having a droplet diameter of about 10 μm to 20 μm is sprayed to be completely evaporated in the cooling tower 36c, the spraying is performed in order to suppress impurities from being deposited from the droplet. It is desirable to use pure water from which impurities are removed to an extremely small amount. When impurities are deposited in the space in the cooling tower 36c, the impurities may adhere to the inner wall or the like of the cooling tower 36c, or extremely small impurities may be introduced into the mainstream air and entrained in the compressor to damage the compressor. Therefore, the spray tower shown in FIG. 8 is configured to spray a large amount of relatively large droplets having a droplet diameter of 100 μm or more from the spray nozzle 93 so that only a part of the surface of the sprayed droplets evaporates. ing. The liquid droplets that do not evaporate and flow into the liquid reservoir are then recirculated by a pump and used again for spraying from the spray nozzle 93. With such a configuration, in the spray tower shown in FIG. 8, impurities in water remain in the droplets without evaporating, so that it is possible to cool impurities without preparing pure water from which impurities have been removed to a very small amount. Adhesion to the inner wall of the tower and inflow into the compressor can be suppressed, and a decrease in cooling efficiency of the cooling tower and a decrease in reliability of the compressor can be suppressed.

  When a packed tower or a perforated plate tower is used as the cooling tower, heat is exchanged with the mainstream air in a state where most of the droplets adhere to the structure such as the packed material 71 and the perforated plate 92. Therefore, the possibility of impurities adhering to the inner wall of the cooling tower and inflow into the compressor is low. However, even in this case, if it is configured to spray droplets of a predetermined size or more, not only the reliability of the compressor can be further improved, but also the structure such as the packing 71, the perforated plate 92, and the mist remover 72 can be applied. The adhesion of impurities can be suppressed, and an increase in pressure loss of mainstream air and a decrease in cooling efficiency can be suppressed without preparing pure water from which impurities are removed to an extremely small amount.

  In the present embodiment, an example in which a packed tower which is the cooling tower 36a shown in FIG. 2 is used as the intermediate cooling mechanism of the compressor is shown. However, instead of the packed tower, the perforated plate tower shown in FIG. The spray tower shown may be used. In short, it is sufficient that the contact area between the mainstream air and the droplets can be increased. By widening the gas-liquid contact area, the efficiency of heat exchange is improved, and efficient evaporation of droplets is promoted, and the cooling tower 36 can be reduced in size and cost. The cooling efficiency of the cooling tower 36 can be further increased.

  Next, the operation method of the cooling tower 36 at the time of starting the gas turbine system of the present embodiment will be described with reference to FIG. Before starting the compressors 10a and 10b, water is injected into the cooling tower 36 to a predetermined water level by the water supply pump 7. Here, the predetermined water level is a design water level that is uniquely determined for each system, and is a water level that can secure at least a water amount that does not cause a shortage of circulating water during operation of the cooling tower. Thereafter, the water in the liquid pool 74 of the cooling tower 36 is supplied to the heat exchanger 90 by the circulation pump 6. The water exchanged with the low-temperature cooling water 91 by the heat exchanger 90 is supplied to the liquid distributor 80 of the cooling tower 36 via the regulating valve 84. The water sprayed on the surface of the filling 71 from the liquid disperser 80 falls into the liquid reservoir 74 and is sucked into the circulation pump 6, and thereafter circulates through the same path.

  In this state, the compressors 10a and 10b are driven by a driving device (not shown). When the compressor is driven, the dew point temperature of the air rises as the pressure rises inside the compressor. When the constituent members of the compressor 10a are low in temperature, moisture in the air is condensed and condensed water is generated. This condensed water is collected by the mist remover 72 of the cooling tower 36 and flows down to the liquid reservoir 74. When the amount of condensed water is large, the water level of the liquid reservoir 74 rises, so that the adjustment valve 39 of the pipe 79 is automatically controlled to discharge excess water out of the system. When the constituent members of the compressor 10a are warmed with the passage of time and the discharge air temperature of the compressor 10a reaches a steady state, the downstream of the intake pipe 85b of the compressor 10b reaches the steady state by the action of the cooling tower 36.

  As described above, the reason why it is desirable to start the air compression after the sprinkling of the packing 71 of the cooling tower 36 is started is to suppress the occurrence of the following two problems. The first problem is that when the cooling tower 36 is sprinkled after starting the compressor, the suction temperature, pressure, and flow rate of the compressor 10b fluctuate rapidly, and the flow rate / pressure ratio of the compressor 10b becomes unstable. The point is that it enters a vibrating surge region, and the reliability of the compressor 10b decreases. Since the compressor 10b is coaxially connected in series with the compressor 10a, the compressor 10a is also affected by the pressure ratio and the flow rate, and the reliability similarly decreases. The second problem is that when the compressor is driven without watering the cooling tower 36, the internal temperature of the cooling tower 36 rises to about 174 ° C., and the equipment and piping also become hot. When water is sprayed in the cooling tower 36 in such a high temperature state, there is a possibility that the pressure rapidly increases due to a sudden boiling phenomenon of the liquid phase water in contact with the high temperature member.

  That is, by starting the air compression after the water sprinkling to the cooling tower 36 is started in advance, a sudden change in temperature, pressure and flow rate in the flow path of the compressor 10 can be avoided. And the fall of the reliability of the cooling tower 36 can be suppressed. In the present embodiment, the mist remover 72 is installed in the cooling tower 36, and even if watering is started before the compressor is started, there is a low possibility that drain will flow into the compressor. Therefore, it is not necessary to newly provide means for suppressing erosion even when watering is started before the compressor is started.

  On the other hand, regarding the operation method of the cooling tower 36 when the gas turbine system of the present embodiment is stopped, it is desirable to stop the water spraying to the cooling tower 36 after stopping the compressors 10a and 10b. When water spraying to the cooling tower 36 is stopped while the compressor is being driven, the discharge temperature, pressure, and flow rate in each of the compressors 10a and 10b change abruptly, causing the compressor surge phenomenon and spray water bumping. This is because there is a possibility. By stopping the compressors 10a and 10b as described above, and then stopping watering to the cooling tower 36, a sudden temperature change and pressure change of the fluid to be compressed while the compressors 10a and 10b are driven can be avoided. It is possible to suppress a decrease in the reliability of the compressor 10 and the cooling tower 36.

  Next, another embodiment of the regeneration cycle gas turbine system provided with the intermediate cooling mechanism of the present invention will be described with reference to FIG. FIG. 4 shows a regenerative cycle gas turbine system equipped with an intermediate cooling mechanism for a compressor according to an embodiment of the present invention. In the regeneration cycle gas turbine system including the intermediate cooling mechanism shown in the first embodiment, the cooling effect of the compressed air is 100 ° C. or higher, and the humidification amount of the compressed air is 0.6% by mass of the air mass. The present embodiment shows a regenerative cycle gas turbine system having an intermediate cooling mechanism in which the cooling effect of compressed air is reduced and the effect of humidification of compressed air is increased as compared with the system shown in the first embodiment. The structural difference between the system shown in this embodiment and the system shown in Embodiment 1 is that the heat exchanger 90 and the cooling water 91 are not used. The discharge water of the circulation pump 6 is supplied to a liquid distributor 80 installed above the packing after the flow rate is adjusted by the adjusting valve 84 without being cooled.

  With reference to FIG. 4, the steady state operation of the intermediate cooling mechanism in the present embodiment will be described. The air compressed to about 400 kPa by the compressor 10a flows into the cooling tower 36 from the discharge pipe 86a. In the cooling tower 36, hot water of about 65 ° C. supplied from the circulation pump 6 is sprayed on the surface of the packing. In the case of atmospheric conditions with an air temperature of 15 ° C. and a relative humidity of 60%, the dew point temperature of the compressed air at the inlet to the cooling tower 36 is about 29 ° C., and the cooling tower is brought into gas-liquid contact with hot water higher than the dew point temperature. At 36, the air is humidified.

  FIG. 6 is a graph showing the distribution of temperature, absolute humidity, and humidification amount with respect to the height direction position in the packing 71 installation portion inside the cooling tower 36 of the present embodiment, where (a) is the temperature, (B) shows absolute humidity, and (c) shows the amount of humidification. As shown in FIG. 6A, about 174 ° C. air (solid line) flowing from the bottom of the cooling tower 36 exchanges heat with about 65 ° C. liquid film (dashed line) flowing down the surface of the packing 71 from above. However, the temperature becomes lower as it flows upward. As shown in FIG. 6B, since the absolute humidity of the humid air on the liquid film surface (broken line) is higher than the absolute humidity of the mainstream air (solid line) in all areas of the packing 71 installation portion, the water vapor pressure difference is driven. As a force, as shown in FIG. 6C, water vapor moves from the liquid film surface into the mainstream air. As a result, the absolute humidity in the mainstream air monotonously increases as it flows upward. In Example 1, since the water of about 35 ° C. was sprayed, the absolute humidity of the mainstream air and the air on the liquid film surface was reversed above the packing, but in this example, it was not reversed. In this embodiment in which hot water of about 65 ° C. is brought into contact with compressed air of about 174 ° C., the humidification amount of the air is 3.2% by mass of the air mass. On the other hand, the air temperature at the exit of the cooling tower is 82 ° C. That is, the air is cooled at about 90 ° C. by the cooling tower 36. The liquid film water dropped from the packing flows down to the liquid pool 74 of the cooling tower 36. Moisture lost due to evaporation is replenished via the feed water pump 7 and the regulating valve 38, and is supplied from the circulation pump 6 to the heat exchanger 90 as hot water of about 65 ° C.

  In the system shown in this embodiment, the evaporation amount is about 3.2% by mass of the air mass and the amount of makeup water in the cooling tower 36 is relatively large, and the evaporation amount is about 0.6% by mass of the air mass. Different from the first embodiment. By increasing the evaporation amount by about 3.2% by mass of the air flow rate, the compressor 10a was able to compress the humid air having a mass flow rate of 103.2% by the compression work required for the mass flow rate of 100%. The compression power per mass flow rate could be reduced.

  The compressed air that has been cooled to about 82 ° C. by the cooling tower 36 and whose mass flow rate has increased by 3.2% is sucked into the compressor 10b from the suction pipe 85b and compressed to about 1600 kPa. The temperature at this time is about 260 ° C. In this embodiment, since the intake air temperature of the compressor 10b is relatively low at about 82 ° C. and the discharge temperature is about 260 ° C., the compression power can be greatly reduced as compared with the case where these temperatures are high. Other operations and functions are the same as those in the first embodiment.

  When the circulating water in the cooling tower 36 is not cooled as in the present embodiment, the intermediate cooling of the compressed air has a larger portion due to the latent heat of evaporation of the spray water than in the first embodiment in which the circulating water is cooled, and the cooling width of the air is humidified. It tends to be restricted by the dew point temperature of the humid air that rises with it. On the other hand, since the heat exchanger 90 used in Example 1 is not required, the equipment cost can be reduced. Further, the more moisture added to the combustion air, the lower the amount of nitrogen oxide produced during combustion.

  The method for starting and stopping the cooling tower 36 in the present embodiment is substantially the same as that in the first embodiment, except that the heat exchanger 90 on the downstream side of the circulating water pump 6 is not started.

  Next, another embodiment of the present invention will be described with reference to FIG. FIG. 9 shows a steam heat pump system equipped with an intermediate cooling mechanism for a compressor according to an embodiment of the present invention. The present embodiment is different from the first and second embodiments in that the fluid flowing through the compressor is not air but water vapor.

  The main components of the present embodiment are driven by an evaporator 42 that evaporates the liquid water 35 by the heat of the hot water 40 introduced from the outside under the condition of atmospheric pressure or less and generates water vapor, and a driving device (not shown). There are compressors 110a, 110b, 110c, and 110d that pressurize water vapor generated by the evaporator 42, and a discharge pipe 25 that supplies high-temperature water vapor pressurized by the compressor 110d to a customer. The compressors 110a, 110b, 110c, and 110d are coaxially connected in series and are configured to gradually increase the water vapor pressure. Further, characteristic components of the present embodiment include a cooling tower 136a connected to the discharge pipe 186a of the compressor 110a, a cooling tower 136b connected to the discharge pipe 186b of the compressor 110b, and a discharge pipe of the compressor 110c. There is a cooling tower 136c connected to 186c. These cooling towers 136a, 136b, and 136c are provided with circulation pumps 6a, 6b, and 6c, respectively, for recirculating the circulating water dropped to the lower part of the tower above the packing 71 in the tower. Further, the replenishing water pump 5 and the regulating valve 83 can supply as much replenishing water 31 to the evaporator 42 as necessary. Liquid water 35 from the evaporator 42 can be supplied to the cooling tower 136a by the feed water pump 7 and the regulating valve 38a. Further, the cooling towers 136b and 136c are respectively piped so as to be able to supply water discharged from the circulation pumps 6a and 6b of the cooling towers 136a and 136b, and regulating valves 38b and 38c are respectively installed in these pipes. . The structures and functions of the cooling towers 136a, 136b, and 136c are substantially the same as those of the cooling tower 36 of the first embodiment. However, when the internal pressure of the cooling tower 36 is lower than the pressure outside the system as in this embodiment, a pressure pump or the like (not shown) is installed in the pipe 79 to make the liquid phase water higher than the pressure outside the system. Discharge.

  Next, the operation method in the steady state of the heat pump system of the present embodiment will be described.

  The evaporator 42 is supplied with hot water 40 heated to about 70 ° C. by an external heat source. Examples of external heat sources to be used include exhaust heat from factories, refuse incineration plants, thermal power generation facilities, internal combustion engines, and the like. The liquid water 35 of the evaporator 42 is maintained at about 63 ° C. by indirect heat exchange with the hot water 40. As a method for maintaining the temperature at about 63 ° C., for example, there is a method of controlling the supply flow rate or temperature of the hot water 40. The liquid level of the liquid water 35 maintained at about 63 ° C. is in a vapor-liquid equilibrium state of about 23 kPa of water vapor having a saturated water vapor pressure of 63 ° C. and about 63 ° C. liquid phase water. The air in the upper space of the evaporator 42 is discharged and becomes a space filled with water vapor having an absolute pressure of about 23 kPa. By driving the compressor 110a in this state, water vapor having a volume corresponding to the suction capacity of the compressor 110a is sucked from the suction pipe 185a. By this suction, the liquid water 35 continuously evaporates on the liquid surface of the liquid water 35 to generate water vapor, and a large amount of latent heat of evaporation is taken away from the liquid water 35. This heat is exchanged with the hot water 40. Be covered.

  The water vapor sucked into the compressor 110a at a temperature of about 63 ° C. and a pressure of about 23 kPa is pressurized to about 48 kPa by the compressor 110a, and becomes a superheated steam at a temperature of about 145 ° C. The superheated steam at about 145 ° C. flows from the gas disperser 70 of the cooling tower 136 a into the cooling tower 136 a and is sprayed from the liquid disperser 80 on the surface of the packing 71, which is a saturation temperature of about 80 ° C. It is in gas-liquid contact with a liquid film of hot water at a lower temperature.

  FIG. 10 is a graph showing the distribution of temperature, flow rate, and vapor pressure with respect to the height direction position in the packing 71 installation portion inside the cooling tower 36 of the present embodiment, where (a) is the temperature, ( b) shows the flow rate, and (c) shows the vapor pressure.

  The sprayed hot water flows down in the form of a liquid film on the surface of the filling 71. As shown in FIG. 10 (a), in the upper region of the filling, the temperature difference from the high-temperature superheated steam The hot water is heated by the heat transfer based on, and becomes hot as it flows downward. The upper limit of the temperature at which hot water is heated is about 80 ° C., which is the saturation temperature of the pressure in the tower. In the lower region of the packing, hot water is heated by superheated steam at about 145 ° C. by heat transfer based on the temperature difference, and hot water at about 80 ° C. flowing down the surface of the packing is heated. This amount of heat is not used for increasing the temperature of hot water because the saturation temperature in the tower is about 80 ° C., but is used as latent heat for evaporating the hot water. As shown in FIG. Part becomes water vapor. This action increases the water vapor mass flow rate by about 5 percent after passing the packing. On the other hand, as the superheated steam is deprived of sensible heat by hot water, the temperature decreases as it flows upward as shown in FIG. When hot water evaporates from the surface of the liquid film, the water that evaporates is pure water vapor that does not contain impurities, and if makeup water contains impurities such as solids, metal ions, and oxides, they are liquid films. Concentrate in water. Therefore, even if impurities are mixed in the make-up water, the steam added to the mainstream steam in the cooling tower 136 does not contain impurities, and therefore the compressors and equipment on the downstream side of the cooling tower 136 are not affected. Absent. If the cooling tower 36 of the present embodiment is used, it is possible to suppress a decrease in the reliability of the compressors and instruments without using make-up water from which impurities are removed to a very small amount.

  The spray water flowing down from the packing reaches about 80 ° C., which is the saturation temperature, and falls into the liquid pool 74 of the cooling tower 136a and is collected. Since the amount of water flowing down decreases due to evaporation as shown in FIG. 10B, the water level is measured by the water level meter 78 and the adjustment valve 38 is automatically controlled to maintain the amount of water in the liquid reservoir 74, and makeup water is supplied from the pipe 75. Supply. By mixing with low-temperature water, the water temperature of the liquid pool 74 is several degrees lower than the saturation temperature of about 80 ° C.

  By this action, the temperature of the superheated steam is reduced to about 80 ° C., which is the saturation temperature in the cooling tower 136, and the flow rate is slightly increased. As the energy change, the sensible heat energy of the superheated steam is converted into latent heat energy, and as a result, the temperature of the water vapor is lowered and the flow rate is increased. Since the compressor 110a only needs the power to compress the steam at the flow rate before the increase, the compressor 110a can compress the steam at a larger mass flow rate with less compression power.

  Due to the shearing force between the liquid film flowing down the surface of the filling 71 and the water vapor flowing upward, a fine mist called entrainment is generated from the surface of the liquid film. The water vapor and fine mist flowing upward in the flow path of the filling 71 flow into the mist remover 72 located above after passing through the filling 71. In the mist remover 72, most of the mist is removed, and the water vapor that has come out of the cooling tower 36a in a state of being dry steam at the saturation temperature flows into the compressor 10b through the pipe 73. Here, the purpose of removing mist is to prevent droplets from colliding with the rotating portion of the compressor and causing mechanical erosion called erosion. When the mists collected by the mist remover are combined with each other to form large droplets, they fall by gravity and flow down the surface of the filling material as spray water.

  In the compressor 110b of the present embodiment, intermediate cooling is performed by the action of the cooling tower 136, thereby compressing steam at a temperature lower than that of a system that does not perform intermediate cooling. Therefore, when compressing with the same pressure ratio, it is possible to compress with less power. The discharge steam of the compressor 110b of the present embodiment is superheated steam having a pressure of about 95 kPa and a temperature of about 158 ° C. When compressing this superheated steam with the compressor 110c, the cooling tower 136b cooled the superheated steam to near the saturation temperature in the same manner as described for the cooling tower 136a to reduce the compression power, and the mass flow rate increased slightly. Adjust to water vapor. Hereinafter, also when compressing by the compressor 110d, the superheated steam is cooled to near the saturation temperature by the cooling tower 136c, and the mass flow rate is increased. As a result, the steam temperature at the inlet of the compressor 110d is about 117 ° C. and the pressure is about 179 kPa, the steam temperature at the outlet of the compressor 110d is about 187 ° C., and the pressure is about 312 kPa. The superheated steam is supplied to the heat utilization facility through the discharge pipe 25 and used.

  In this embodiment, due to the action of the cooling towers 136a, 136b, and 136c, the compressors 110b, 110c, and 110d have the effect of compressing steam with a larger mass flow rate with less compression power. Since the saturated steam at a lower temperature is compressed, it can be compressed with less power. As a whole system, more water vapor can be compressed with less power, and the efficiency increases synergistically.

  The effect of the present embodiment will be described quantitatively with reference to FIG. FIG. 11 shows changes in temperature, pressure, and mass flow rate when the cooling tower of this embodiment is operated and not operated, where (a) is the temperature, (b) is the pressure, (c ) Indicates mass flow rate.

  The temperature of the discharge pipe 186d of the compressor 110d is about 187 ° C. as shown by the solid line in FIG. 11A when the cooling tower is operated, whereas it is a broken line when the cooling tower is not operated. As shown in FIG. Therefore, when the same compressor is used, the discharge pressure of the former is about 312 kPa, whereas the latter can only rise to about 206 kPa. Since general industrial steam is used as saturated steam, the utility value of steam is greatly different between about 312 kPa and about 206 kPa. Furthermore, in this embodiment, an effect of increasing the amount of water vapor as a working medium can be obtained. When the cooling tower 136 is operated, the amount of water vapor is 1.17 times, whereas when the cooling tower 136 is not operated, the increase amount is zero.

  In order to prevent the impurities contained in the makeup water from concentrating and deteriorating the water quality of the liquid reservoir 74, as in the first and second embodiments, the regulating valve 39 is operated continuously or It is desirable to intermittently discharge part of the liquid phase water out of the system.

  Further, in this embodiment, it is planned to use a water source having a temperature as close as possible as a supply water source to the liquid pool 74 of the cooling towers 136a, 136b, and 136c. May be. In this case, the basic operation is almost the same. However, since the temperature of sprinkling water from each liquid disperser 80 is lowered, the sensible heat taken from the superheated steam is increased and the amount of new water vapor generated is reduced, but the cooling effect of the mainstream water vapor is enhanced.

  As described above, according to the present embodiment, the steam compressor 110 can provide an intermediate cooling mechanism that is compact and low-cost and does not require pure water from which impurities are removed to an extremely small amount. Furthermore, since the thermal energy possessed by the superheated steam can be converted into the mass energy of the steam, the efficiency of the entire system can be increased.

  Although the mechanical pump is assumed in this embodiment as the circulation pump 6 and the water supply pump 7, a steam jet pump can be configured by using higher-pressure steam in the discharge pipe 25 and the discharge pipe 186. is there. In this case, the device can be simplified, and the possibility of fluid leakage from the shaft seal portion and mixing of impurities from the outside can be reduced as compared with a mechanical pump.

  Next, a startup method of the steam heat pump system of this embodiment will be described. Before starting the compressors 110a, 110b, 110c, and 110d, water is injected into the cooling towers 136a, 136b, and 136c to a predetermined water level. After the water injection is completed, the regulating valves 84a, 84b, and 84c are opened, water is sprayed into the packing 71 of the cooling towers 136a, 136b, and 136c, and water is supplied in the respective cooling towers by the circulation pumps 6a, 6b, and 6c. Circulate.

  In this state, the compressors 110a, 110b, 110c, and 110d are driven, and the air existing in the suction pipe 185, the discharge pipe 186, and the cooling tower 136 is exhausted from the discharge pipe 25 by the fluid driving action of the compressor. It is gradually discharged into the atmosphere via the stack. At this time, instead of driving the compressors 110a, 110b, 110c, and 110d, air may be discharged using a vacuum pump (not shown). If it is designed so that the air is discharged by the compressor 110, an exhaust vacuum pump is unnecessary. On the other hand, if the exhaust vacuum pump is designed to discharge air, the compressor 110 can be designed exclusively for low-pressure steam, and a compressor that exhibits high performance during steady operation can be applied. When the compressor 110 discharges air, it is necessary to design the flow rate / pressure ratio characteristics of the compressor so that an unstable event such as a surge does not occur when compressing not only water vapor but also air. Because.

The upper space of the evaporator 42 becomes a space filled with water vapor having an absolute pressure of about 23 kPa after the air is discharged. Further, in the cooling towers 136a, 136b, and 136c, when the compressors 110a, 110b, 110c, and 110d are driven, the temperature and pressure reach a steady state and the start-up is completed. During this time, in the process of increasing the temperature, the heat of the steam is used to raise the temperature of the cooling tower 136, the suction pipe 185, and the discharge pipe 186, which were low in temperature, and some of the steam is condensed. This condensed water is collected by the mist remover 72 of the cooling tower 136 and flows down to the liquid reservoir 74.
When the amount of water vapor condensation is large at the time of startup, the water level of the liquid pool 74 rises, so that the control valve 39 of the pipe 79 is automatically controlled to discharge the liquid phase water out of the system.

  As described above, it is desirable that the compression of the water vapor is started after the sprinkling of the packing 71 of the cooling tower 136 is started. The reason for this is to suppress the occurrence of the following two problems. The first problem is that when the cooling tower is sprinkled after starting the compressor, the discharge temperature, pressure, and flow rate of each of the compressors 110a, 110b, 110c, and 110d change rapidly, and the flow rate / pressure ratio of the compressor. May enter a surge region that oscillates in an unstable manner, reducing the reliability of the compressor. The second problem is that when the compressor is driven without watering the cooling tower, the water vapor temperature of the cooling tower 36c on the most downstream side is about 300 ° C., and the equipment and piping are also hot. When sprinkling is started in the cooling tower 136 in such a high temperature state, there is a possibility that a sudden boiling phenomenon may occur due to a sudden boiling phenomenon of liquid phase water in contact with the high temperature member. As in the present embodiment, by starting the compression of the water vapor after starting the water spraying to the cooling tower 136 in advance, it is possible to avoid a sudden change in temperature, pressure, and flow rate in the water vapor flow path. High performance driving can be performed.

  On the other hand, when the steam heat pump system of the present embodiment is stopped, it is desirable to stop the water spraying to the cooling tower 136 after the procedure opposite to the start-up, that is, the compressor is stopped. When water spraying to the cooling tower 136 is stopped while the compressor is being driven, the discharge temperature, pressure, and flow rate of water vapor in each of the compressors 110a, 110b, 110c, and 110d change abruptly to the compressor surge region. This is because there is a possibility that the transition of water and bumping of watering may occur.

  As in this embodiment, by stopping the water spraying to the cooling tower 136 after stopping the compressor, abrupt changes in temperature, pressure, and flow rate of the fluid to be compressed can be avoided during driving of the compressor. Can be operated with high reliability.

  In each embodiment, a plurality of compressors are used and the cooling tower 36 and the cooling tower 136 are provided between the compressors. However, the present invention is not limited to the case where a plurality of compressors are used. Any compressor can be used as long as it has a plurality of stages. When a multi-stage compressor is used, if the cooling tower 36 and the cooling tower 136 are provided between the stages of the compressor, the same effects as those shown in the embodiments can be obtained.

  5 ... makeup water pump, 6, 6a, 6b, 6c ... circulation pump, 7 ... feed water pump, 10a, 10b, 110, 110a, 110b, 110c, 110d ... compressor, 12 ... combustor, 14 ... turbine, 16 ... Generator, 25, 86, 86a, 86b, 186, 186a, 186b, 186c, 186d ... discharge pipe, 31 ... makeup water, 35 ... liquid water, 36, 36a, 36b, 36c, 136, 136a, 136b, 136c, 136d ... Cooling tower, 38, 39, 83, 84 ... Regulating valve, 40 ... Warm water, 42 ... Evaporator, 50 ... Fuel, 60 ... Regenerative heat exchanger, 61 ... Outlet piping, 70 ... Gas distributor, 71 ... Packing 72 ... Mist remover, 74 ... Liquid reservoir, 75, 76, 79 ... Piping, 78 ... Water level gauge, 80 ... Liquid disperser, 82 ... Stack, 85, 85a, 85b, 185, 185a, 1 5b, 185c, 185d ... suction pipe, 90 ... heat exchanger, 91 ... cooling water, 92 ... perforated plate, 93 ... spray nozzle.

Claims (6)

A first compressor for compressing the working fluid;
A first intercooler for cooling the working fluid compressed by the first compressor by direct contact heat exchange with water;
A second compressor for compressing the working medium cooled by the first intercooler;
A second intercooler that cools the working medium compressed by the second compressor by direct contact heat exchange with water;
A third compressor for compressing the working medium cooled by the second intercooler,
A system comprising: a system for supplying water to the first intermediate cooler; and a system for supplying water from the first intermediate cooler to the second intermediate cooler. A plurality of compressors for compressing the working medium;
A system comprising a plurality of intermediate coolers provided between the plurality of compressors and cooling the working medium by direct contact heat exchange with water,
A system for supplying water to an intermediate cooler provided in the uppermost stream in the flow direction of the working medium among the plurality of intermediate coolers, and an intermediate cooling provided downstream from the intermediate cooler provided in the uppermost stream A system characterized by having a system for supplying water to the vessel. A water supply system for supplying water;
An evaporator for evaporating water supplied from the supply system to generate steam;
A first compressor for compressing the steam generated in the evaporator;
A first intercooler that cools the steam compressed by the first compressor by direct contact heat exchange with water;
A second compressor for compressing the steam cooled by the first intercooler;
A second intercooler for cooling the steam compressed by the second compressor by direct contact heat exchange with water;
A third compressor for compressing the steam cooled by the second intercooler;
A heat pump system comprising a steam supply system for supplying steam compressed by the third compressor to a steam utilization facility,
A heat pump system comprising a system for supplying water from the first intermediate cooler to the second intermediate cooler. In the system or heat pump system according to claim 1-3,
The intermediate cooler is supplied so as to be cooled by spraying a liquid of a desired amount or more, and is configured such that spray water remaining without evaporating flows down to a liquid pool. . The system or heat pump system according to claim 4,
A system or heat pump system characterized in that a part of the water sprayed by the intermediate cooler is recovered and the recovered liquid can be sprayed again. A first compressor for compressing the working fluid;
A first intercooler for cooling the working fluid compressed by the first compressor by direct contact heat exchange with water;
A second compressor for compressing the working medium cooled by the first intercooler;
A second intercooler that cools the working medium compressed by the second compressor by direct contact heat exchange with water;
A method of cooling a working medium in a system comprising a third compressor for compressing the working medium cooled by the second intercooler,
A method of cooling a working medium, comprising supplying water extracted from the first intermediate cooler into the second intermediate cooler and cooling the working medium compressed by the second compressor.

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