JP5813344B2 - Waste heat recovery power plant for sintering equipment - Google Patents

Description

  The present invention relates to a waste heat recovery power plant that is applied to a sintering facility that includes a sintering machine and a sintered ore cooler and generates sintered ore.

  The iron ore used in steelworks is mainly powdered ore that is made by blending powdered iron ore with respect to the origin and properties, and homogenizing it. However, when the powdered ore is charged into the blast furnace as it is, it becomes clogged and reduced gas. Obstruct the flow. Therefore, it is often the case that a small amount of lime powder and coke are mixed in advance with powdered ore, and baked and hardened to a certain size using a sintering machine to form a massive sintered ore. Currently, in Japan, it is said that sintered ore accounts for almost 75% of the iron ore charged in the blast furnace.

  Sintered ore is a mixture of granulated ore, limestone, and powdered coke and granulated. The sintered raw material is charged into a sintering machine and ignited, and sucked while the sintered raw material moves toward the end by a conveyor. The air sucked by the blower is blown from the top to the bottom to burn the powder coke, and the powdered ore is partially melted and combined with the heat of combustion of the coke, and then crushed and selected to have a diameter of 15 to 30 mm. Obtain sinter. The high-temperature sinter produced by the sintering machine is transferred to a sinter cooler and is cooled to a temperature at which it can be stored by applying a cooling airflow from below the conveyor while being conveyed by the conveyor.

As described above, a sintering facility for producing sintered ore includes a sintering machine and a sintered ore cooler. In the sintering machine, air is supplied to burn the sintering raw material, and the gas generated by the combustion becomes exhaust gas distributed from a low temperature of about 50 to 60 ° C. at the ignition portion to a high temperature of about 400 to 450 ° C. at the end portion of the conveyor. Moreover, since a high-temperature sintered ore is cooled with air in a sintered ore cooler, the cooling air becomes a high-temperature exhaust gas of 300 to 400 ° C.
Conventionally, as shown in FIG. 3, for example, as for the exhaust gas of the sintered ore cooler, surplus heat of the exhaust gas is recovered by a waste heat boiler to generate steam, and as utility steam or electric power obtained via a steam turbine Waste heat is effectively recovered.

Incidentally, Patent Document 1 discloses an improved invention in a waste heat recovery method for generating electric power by supplying steam generated by introducing cooling air heated by a sinter cooler to a waste heat boiler to a steam turbine. ing.
The waste heat recovery method for a sinter cooler disclosed in Patent Document 1 is divided into a boiler communication region where the sinter ore is in a higher temperature state and a flue communication region where the cooling progresses, After cooling, the cooling gas introduced into the communication area is guided to the boiler through a hood that covers the sintered ore after cooling, and the heat is recovered. The cooling gas introduced into the flue communication area guides the exhaust gas after cooling to the flue as it is to the atmosphere. In this method, the inside of the hood is always kept at a positive pressure so that the atmosphere does not enter, and the temperature of the recovered cooling gas is prevented from being lowered, and the partition between the boiler communication area and the flue communication area can be arbitrarily set. Thus, the heat recovery rate is improved.
In Patent Document 1, there is no mention or suggestion of recovering and using surplus heat generated in the sintering machine.

  By the way, in a cement firing plant equipped with a suspension preheater (PH) and an air quenching cooler (AQC), conventionally, exhaust gas of PH is recovered by heat in a boiler and used for drying cement raw material, and the exhaust gas of AQC is limited by the boiler. Waste heat power generation systems that recover heat and generate electricity have been used. The temperature of the exhaust gas of PH is, for example, 350 to 400 ° C., and the temperature of the exhaust gas of AQC is, for example, 300 to 250 ° C., but the amount of the exhaust gas is larger than PH.

On the other hand, for example, Patent Document 2 discloses a waste heat power generation system that recovers PH waste heat and AQC waste heat with a waste heat boiler to obtain steam and drives a steam turbine to generate power. Yes.
The cement firing plant waste heat power generation system disclosed in Patent Document 2 converts a part of hot water heated by the AQC boiler economizer into low-pressure steam through a flasher and puts it into the low-pressure stage of the steam turbine. The remaining part is superheated through the evaporator and superheater of the AQC boiler, and the rest is superheated through the evaporator and superheater of the PH boiler, and the generated high-pressure steam is introduced into the high-pressure stage of the steam turbine.

  As shown in FIG. 4, the waste heat power generation system of Patent Document 2 includes a second evaporator having a steam drum on the exhaust gas outlet side of the PH boiler, and the return hot water from the flasher passes through the steam drum. The hot water introduced into the second evaporator and heated by the second evaporator is returned to the steam drum, and the steam generated in the steam drum is introduced into the low pressure stage of the steam turbine.

The disclosed waste heat power generation system maintains the outlet gas temperature of the AQC boiler as low as possible, while making the PH boiler two pressures to supply steam suitable for each of the high-pressure stage and the low-pressure stage of the multi-stage steam turbine. Thus, the outlet gas temperature of the PH boiler is made as low as possible to greatly increase the waste heat recovery rate.
In the disclosed system, the PH boiler inlet gas temperature 325 ° C. is lowered to the outlet gas temperature 165 ° C., and the AQC boiler inlet gas temperature 360 ° C. is lowered to the outlet gas temperature 105 ° C.
In this manner, the disclosed waste heat power generation system can fully recover the waste heat of AQC, and can fully utilize the waste heat of PH to be converted into electric energy.

  Therefore, if we applied the technical idea of the cement firing plant waste heat power generation system to the sintering equipment equipped with a sintering machine and a sinter cooler, we were able to effectively use the waste heat of the sintering machine. The sintering machine boiler (SM boiler) corresponding to the PH boiler is adopted as the sintering machine, and the sintered ore waste heat boiler (SC boiler) corresponding to the AQC boiler is adopted as the sintering ore cooler.

However, in the sintering machine, sulfur component contained in the sintering raw material is oxidized during the sintering process to become sulfurous acid gas SO ₂ , and further oxidized to form anhydrous sulfuric acid SO ₃ is contained in the exhaust gas. Therefore, when the temperature of the exhaust gas falls below the acid dew point, the gas that has become sulfuric acid due to the reaction of SO ₃ with water vapor condenses, and droplet sulfuric acid appears on the solid surface and exhibits high corrosiveness. There is a risk of damaging the exhaust gas treatment device and the flue provided in the flow path in the middle of the exhaust gas flow.

For this reason, normally, the exhaust gas at the exhaust gas smoke outlet is determined in consideration of the acid dew point. The acid dew point of sulfuric acid is a value that depends on the partial pressure of SO _{3 and} the partial pressure of water, but is about 120 to 140 ° C., so that the exhaust gas temperature should be about 140 to 150 ° C., for example. preferable.

Also, when the exhaust gas containing sulfuric acid gas reaches a temperature below the dew point of water, sulfuric acid dissolves in the condensed water to form a sulfuric acid solution, and the attached metal surface is severely corroded.
For this reason, it is preferable that the exhaust gas in the flue be higher than the dew point temperature of water. The water dew point is a value that depends on the partial pressure of water vapor in the gas, but is approximately 60 to 80 ° C., so that the exhaust gas temperature is preferably maintained at 100 ° C. or higher, for example.

  In addition, when an SM boiler is installed, the exhaust gas from the SM boiler outlet merges with the low-temperature exhaust gas generated in the ignition part of the sintering machine that does not pass through the waste heat boiler, and then passes through the exhaust gas treatment device such as a dust collector to the atmosphere from the chimney. Will be discharged. Therefore, if the exhaust gas temperature after merging does not fall below the acid dew point, exhaust system facilities such as flues will be significantly corroded, so that the exhaust gas temperature after merging is required to be maintained above the acid dew point. Therefore, the exhaust gas at the outlet of the SM boiler is preferably as high as possible in order to meet the combustion gas in the low temperature region in the sintering machine.

  The waste heat boiler disclosed in Patent Document 2 aims at effective waste heat recovery by lowering the exhaust gas temperature at the outlet. Therefore, when the waste heat boiler is introduced into the sintering machine according to the conventional technology, the exhaust gas temperature condition required for the sintering machine waste heat boiler cannot be satisfied, and the exhaust gas is excessively cooled to the exhaust gas treatment system. It will cause obstacles. As described above, the cement firing plant waste heat power generation system cannot be applied as it is, and the waste heat from the sintering machine cannot be effectively recovered.

JP 2000-226618 A JP 2008-157183 A

  Therefore, the problem to be solved by the present invention has not been able to be sufficiently utilized in the past while suppressing the sulfation of anhydrous sulfuric acid contained in the exhaust gas of the sintering machine in addition to the recovery of waste heat in the sinter cooler. An object is to provide a waste heat recovery power plant for a sintering facility that effectively recovers the waste heat of the sintering machine and improves the waste heat recovery rate of the sintering facility.

A waste heat recovery power plant for a sintering facility of the present invention that solves the above problems is a waste heat recovery power plant applied to a sintering facility including a sintering machine and a sintered ore cooler, and an evaporator and a economizer the superheater and the sinter cooler waste heat boiler comprises a steam drum by introducing Atsushi Ko of exhaust gas that occurs in the sintering completion region of a sintered ore cooler for generating hot water and steam, evaporator and superheater And a steam drum, which introduces exhaust gas from the sintering machine to generate steam, a multistage steam turbine combined with a generator, and a high-stage flasher that is a first stage flasher in multiple stages A two-stage flasher that supplies the steam of the low-pressure stage flasher, which is the second-stage flasher, to the low-pressure stage of the multi-stage steam turbine.

  Further, the condensate of the steam turbine and the return hot water of the low pressure stage flasher are heated by the economizer of the sintered ore cooler waste heat boiler, and a part of the heated hot water is steamed from the sintered ore cooler waste heat boiler. The remaining part is supplied to the steam drum of the sintering machine waste heat boiler, the rest is supplied to the high-pressure stage flasher, and the steam generated in the evaporator and superheater of the sinter cooler waste heat boiler The steam generated in the evaporator and superheater of the waste heat boiler of the sintering machine is supplied to the high pressure stage of the multistage steam turbine.

As a result, the exhaust gas at the exhaust gas outlet of the sintering machine waste heat boiler is maintained at a temperature higher than the acid dew point, and the exhaust gas at the place where the exhaust gas of the sintering machine waste heat boiler and the exhaust gas of the sintering machine are combined from the water dew point. High temperature can be maintained.
For example, the exhaust gas in place to hold the exhaust gas in the exhaust gas outlet of the sintering machine waste heat boiler to 200 ° C. or higher and the low temperature exhaust gas merging to occur in the ignition region of the exhaust gas and the sintering machine of the sintering machine waste heat boiler If, for example, is maintained at 160 ° C. or higher, sulfuric acid corrosion can be effectively suppressed.

In the waste heat recovery power plant for sintering equipment according to the present invention, by installing a sintering machine waste heat boiler, the waste heat of the sintering machine is used to suppress steam corrosion due to the exhaust gas of the sintering machine. The high pressure steam supplied to the high pressure stage of the turbine can be replenished. Moreover, in order to maintain the exhaust gas temperature at the outlet in the waste heat boiler of the sintering machine above the acid dew point, it is not possible to sufficiently recover the waste heat, but instead, the production volume of high-pressure steam in the waste heat boiler of the sinter ore cooler By using the reduced pressure for medium pressure steam production in the high pressure stage flasher of the two-stage type flasher, the medium pressure steam is supplied to the middle pressure stage of the steam turbine to supplement the output, thereby using waste heat as a whole. The rate can be improved.
The waste heat recovery power plant for sintering equipment of the present invention can achieve a waste heat recovery rate of about 1.5 times that in the case where the waste heat of the sintering machine is not recovered.

  The waste heat recovery power plant for a sintering facility according to the present invention further includes a economizer in the waste heat boiler for the sintering machine, and supplies the condensate of the steam turbine and the return hot water of the two-stage flasher to the sintered ore cooler. Instead of heating in the waste heat boiler's economizer and supplying it to the steam drum of the sintering machine's waste heat boiler, the hot water of the high-pressure stage flasher is heated in the economizer of the sintering machine's waste heat boiler. It may be one that supplies the steam drum and returns the rest to the high-pressure stage flasher.

Thus, the exhaust gas at the exhaust gas outlet of the sintering machine waste heat boiler is maintained at a temperature higher than the acid dew point, and the exhaust gas when the exhaust gas of the sintering machine waste heat boiler and the exhaust gas of the sintering machine merge is at a temperature higher than the water dew point. And sulfuric acid corrosion can be suppressed.
In addition, the waste heat of the sintering machine is used to replenish high-pressure steam supplied to the high-pressure stage of the steam turbine, and the low-pressure steam generated by the low-pressure stage flasher by using a two-stage flasher is used for the low-pressure stage of the steam turbine. In addition to the above, by supplementing the output of the steam turbine by supplementing the intermediate pressure steam produced by the high pressure stage flasher to the intermediate pressure stage, the utilization rate of waste heat can be improved as a whole by utilizing a low temperature medium. .

  The waste heat recovery power plant for sintering equipment of the present invention generates power by recovering waste heat generated in a sintering machine that could not be recovered sufficiently while suppressing sulfuric acid corrosion by the exhaust gas of the sintering machine, The waste heat utilization rate as a whole can be improved.

It is a block diagram of the waste heat recovery power plant for sintering equipment concerning the 1st example of the present invention. It is a block diagram of the waste heat recovery power plant for sintering facilities which concerns on 2nd Example of this invention. It is a block diagram which shows the example of the conventional waste heat recovery power plant for sintering facilities. It is a block diagram which shows the example of the waste-heat recovery electric power generation system applied to the conventional cement baking plant.

  Hereinafter, embodiments of the present invention will be described with reference to the drawings. In the drawings with different figure numbers, the same reference numerals are assigned to the components having the same functions to facilitate understanding.

FIG. 1 is a block diagram of a waste heat recovery power plant for a sintering facility according to a first embodiment of the present invention. In the figure, the directed solid line indicates the flow of hot water or steam, and the directed dotted line indicates the flow of exhaust.
The waste heat recovery power plant for the sintering facility of the first embodiment is a waste heat that recovers the waste heat generated in the sintering machine (SM) 1 and the sintered ore cooler (SC) 2 in the sintering facility to obtain electric power. It is a recovery power plant.

  For example, the most common Dwight-Lloyd type sintering machine 1 includes a sintered raw material in which a granulated material having a diameter of 2 to 3 mm, powdered limestone as a solvent and powdered coke as a fuel are mixed and granulated. It is put into an iron pallet and ignited. While the sintered raw material of the pallet moves toward the end, the air generated by sucking with the exhaust fan 7 is passed from top to bottom to combust the powder coke, and the combustion heat of the coke. The molten ore is partially melted and bonded to obtain a sintered ore. The sintered ore is crushed and sorted to obtain a sintered ore having a diameter of 15 to 30 mm, and then charged into the sintered ore cooler 2.

The temperature of the exhaust gas generated by burning the sintering raw material in the sintering machine 1 is distributed from a low temperature of about 50 to 60 ° C. in the ignition region to a high temperature of about 400 to 450 ° C. in the sintering completion region.
Further, the exhaust gas in the sintering machine 1 includes sulfurous acid gas SO ₂ generated by oxidizing sulfur components contained in powder coke and iron ore and anhydrous sulfuric acid SO ₃ generated by further oxidizing sulfurous acid gas. When the temperature of the exhaust gas containing anhydrous sulfuric acid SO ₃ drops below the acid dew point, the sulfuric acid droplets form condensation on the solid surface and become highly corrosive, and the heat transfer surface and flue of the heat exchanger are exposed. Since there is a risk of damaging the provided dust collector 3 and the like, it is necessary to keep the temperature of the exhaust gas above the acid dew point.

The high-temperature sintered ore produced by the sintering machine 1 is cooled by circulating cooling air from below the conveyor while being transferred to the sintered ore cooler 2 and conveyed by the conveyor.
The cooling air used for cooling the high-temperature sintered ore with the sintered ore cooler 2 becomes a high-temperature exhaust gas of 300 to 400 ° C.
The exhaust gas of the sinter cooler 2 contains dust because it passes through the crushed sinter, so that it is discharged to the atmosphere after the dust is removed by a dust removing device such as the dust collector 4.

  The waste heat recovery power plant for sintering equipment according to the present embodiment is attached to the sintering equipment having the above-described configuration, and includes a power generator 50 including a steam turbine 51, a power generator 52, and a condenser 53, and sintering. A two-stage type comprising an ore cooler waste heat boiler (SC boiler) 30, a sintering machine waste heat boiler (SM boiler) 10, a high pressure stage flasher 41 as a first stage flasher and a low pressure stage flasher 42 as a second stage flasher. The flasher 40 includes a water supply pump 54 that supplies condensate.

  The SC boiler 30 has the same configuration as that conventionally used, and includes a boiler body 31. The boiler body 31 includes a superheater 33, an evaporator 35, and a economizer 37, and a steam drum 36 is attached. The boiler body 31 is supplied with cooling air heated to 300 to 400 ° C. by the sinter cooler 2. The high-temperature cooling air is efficiently heat-exchanged by the superheater 33, the evaporator 35, and the economizer 37 to heat and cool water or steam, and is discharged from the outlet of the boiler body 31.

  The SM boiler 10 includes a boiler body 11, the boiler body 11 includes a superheater 13 and an evaporator 15, and a steam drum 16 is attached. After being sucked into the boiler body 11 by the exhaust fan 9, a high-temperature portion of the exhaust gas of the sintering machine 1 is introduced, and is efficiently cooled by exchanging heat between the superheater 13 and the evaporator 15. And discharged from the outlet of the boiler body 11. The exhaust gas discharged from the SM boiler 10 is guided to a pipe, merges with a low-temperature portion of the exhaust gas of the sintering machine 1, passes through the dust collector 3, and is discharged from the chimney 5 to the atmosphere.

The steam turbine 51 of the power generation apparatus 50 is a multi-stage steam turbine, and at least outputs a high-pressure stage that supplies high-pressure steam, a low-pressure stage that supplies low-pressure steam to supplement the output, and supplies medium-pressure steam that is intermediate in pressure. Complementary intermediate pressure stage. A generator 52 is directly connected to the steam turbine 51 to convert the kinetic energy of the rotating shaft of the steam turbine 51 into electric power.
The steam that has finished work in the steam turbine 51 is condensed in the condenser 53 and returned to water, and then supplied again to the boiler by the feed water pump 54.

  The high-pressure stage flasher 41 of the two-stage flasher 40 separates steam from the hot water supplied from the SC boiler 30, supplies the generated steam to the middle stage of the steam turbine 51, and supplies the remaining hot water to the low-pressure stage flasher 42. Supply. The low pressure stage flasher 42 separates the low pressure steam from the hot water supplied from the high pressure stage flasher 41, supplies the steam to the low pressure stage of the steam turbine 51, and discharges the remaining hot water from the bottom outlet to the piping system. .

The condensate from the multistage steam turbine 51 and the return hot water from the low-pressure stage flasher 42 are supplied to the economizer 37 of the SC boiler 30 and heated. The heated hot water is distributed to the high-pressure stage flasher 41, the steam drum 16 of the SM boiler 10, and the steam drum 36 of the SC boiler 30.
The hot water supplied to the steam drum 36 of the SC boiler 30 is heated by the evaporator 35 to become high-pressure water and returns to the steam drum 36 for gas-liquid separation. The steam on the steam drum 36 is heated to the saturation temperature or higher by the superheater 33 and becomes high-pressure steam.

Further, the hot water supplied to the steam drum 16 of the SM boiler 10 becomes the same high-pressure steam by the evaporator 15 and the superheater 13, and merges with the high-pressure steam generated by the SC boiler 30. Supplied to the high pressure stage.
At this time, in order to prevent corrosion due to sulfuric anhydride in the exhaust gas, it is necessary to maintain the exhaust gas temperature at the exhaust gas outlet of the SM boiler 10 at, for example, 160 ° C. or higher, which is higher than the acid dew point. Therefore, the amount of waste heat recovered in the SM boiler 10 is limited by the exhaust gas temperature and the exhaust gas flow rate supplied to the SM boiler 10.

  If the pressure or temperature of the steam supplied from the SM boiler 10 to the high pressure stage of the steam turbine 51 is determined, the steam drum 16 of the SM boiler 10 is transferred from the economizer 37 of the SC boiler 30 based on the recovered heat quantity determined as described above. The temperature and flow rate of hot water supplied to the are determined.

  Furthermore, the high pressure stage flasher 41 to which hot water is supplied from the economizer 37 of the SC boiler 30 evaporates, for example, 10% of the supplied hot water and supplies it to the intermediate pressure stage of the steam turbine 51, and the remaining hot water. Is supplied to the low-pressure stage flasher 42. Also in the low pressure stage flasher 42, for example, 10% of hot water can be vaporized and supplied to the low pressure stage of the steam turbine 51. The hot water remaining in the low pressure stage flasher 42 is supplied again to the SC boiler 30 by the feed water pump 54 together with the condensate of the steam turbine 51 generated by the condenser 53 as return hot water.

  The cooling air that has been heated by cooling the sinter with the sinter cooler 2 is guided to the SC boiler 30, recovered by waste heat, cooled, and then discharged from the chimney 6 through the dust collector such as the dust collector 4. Although the air cooled by the SC boiler 30 is partially returned to the sintered ore cooler 2 and used again for cooling, the power for taking in outside air can be reduced.

  In the waste heat recovery power plant configured in this way, the amount of hot water or steam circulating in the power generation system can be increased by the amount of waste heat recovered in the SM boiler 10, so that power generation efficiency is improved. However, since the exhaust gas temperature at the outlet of the SM boiler 10 is limited, in order to obtain high-pressure steam that can be used in the steam turbine 51, the steam drum 16 of the SM boiler 10 is connected to the economizer 37 of the SC boiler 30. It is preferable to supply hot water heated to an appropriate temperature.

In this way, a part of the amount of heat recovered by the SC boiler 30 is used for the SM boiler 10, so that the flasher steam is reduced by this amount. However, by evaporating and heating the SM boiler 10, the steam turbine 51 As a result, the amount of high-pressure steam supplied to the battery increases, so that the overall power generation system is more efficient.
Further, in addition to the conventional method in which the steam generated by the flasher is supplied to the low pressure stage of the steam turbine 51 to increase the output, the SC boiler 30 generates steam that matches the intermediate pressure stage of the steam turbine 51 to generate the steam turbine. In order to reinforce the power by injecting into the intermediate pressure stage 51, a high-pressure stage flasher 41 is newly introduced to make the flasher a two-stage flasher 40, and the high-pressure stage flasher 41 is heated by the economizer 37. The heated water is supplied to increase the output of the steam turbine 51.

For example, in a sintering facility that generates 200,000 Nm ³ / h exhaust gas in the sintering machine 1 and generates 400,000 Nm ³ / h exhaust gas in the sinter cooler 2, the exhaust gas temperature supplied to the SM boiler 10 Is 350 ° C., and the exhaust gas temperature at the outlet is kept above the acid dew point.
For this purpose, for example, the temperature of hot water at the outlet of the economizer 37 of the SC boiler 30 is set to 177 ° C., and water is supplied to the steam drum 16 of the SM boiler 10, so that the water side temperature of the evaporator 15 is 182 ° C. The exhaust gas temperature at the outlet of the SM boiler 10 at this time can be maintained at about 200 ° C.

The acid dew point of sulfuric acid depends on the partial pressure of SO _{3 and} the partial pressure of water, but is approximately 120 to 140 ° C. here. The exhaust gas temperature at the outlet of the SM boiler 10 has a margin of 60 to 80 ° C. up to the acid dew point temperature. Further, the exhaust gas temperature at the position where it joins the low-temperature exhaust gas discharged from the sintering machine 1 can also be maintained at about 100 ° C. higher than the water dew point. Therefore, droplet sulfate sulfation of sulfuric anhydride SO ₃ contained in the exhaust gas and aqueous solution of the sulfuric acid component can be suppressed, and corrosion of the heat transfer surface of the waste heat boiler and the exhaust system equipment can be prevented.

  In the high-pressure stage flasher 41, when flashing at 0.4 MPa, 10% becomes steam and 90% becomes hot water, so steam is supplied to the intermediate pressure stage of the steam turbine 51 and hot water is supplied to the low-pressure stage flasher. 42. The low-pressure stage flasher 42 is flushed at 0.13 MPa, and the supplied hot water is divided into 10% steam and 90% water, and the steam is supplied to the low-pressure stage of the steam turbine 51 to return water to the return heat. Water is supplied to the SC boiler 30 together with the condensate from the condenser 53 as water.

By adopting a two-stage flasher, steam at two pressure and temperature levels can be generated, so that higher temperature steam having high potential can be utilized.
By operating the waste heat recovery power plant of this example under the above conditions and adding waste heat recovered from the exhaust gas of the sintering machine, compared with the case of only waste heat recovery from the sinter cooler As a result, it was possible to obtain approximately 1.5 times the power.

By using the waste heat recovery power plant of the present embodiment, waste heat is removed from the exhaust gas generated in the sintering machine 1 while suppressing damage to various devices in the exhaust gas pipeline due to anhydrous sulfuric acid generated in the sintering machine 1. It can be recovered and used to operate a more efficient sintering facility.
The waste heat recovery power plant of this embodiment has a water supply system shared by the SM boiler 10 and the SC boiler 30 and has the advantage that the equipment cost is low and simple operation is possible. Suitable when there is relatively little possible waste heat.

FIG. 2 is a block diagram of a waste heat recovery power plant for a sintering facility according to a second embodiment of the present invention. In the figure, elements having the same functions as those in FIG. 1 are denoted by the same reference numerals as those in FIG.
Compared with the waste heat recovery power plant of the first embodiment, the waste heat recovery power plant for sintering equipment of the second embodiment is further provided with a economizer 17 in the sintering machine waste heat boiler (SM boiler) 10. Instead of supplying the hot water supplied from the economizer 37 of the sintered ore cooler waste heat boiler (SC boiler) 30 directly to the steam drum 16 of the SM boiler 10, the piping system is slightly changed. 41 and the SM boiler 10 are supplied to the steam drum 16 via the economizer 17, and there is no significant difference in other configurations.

  In the waste heat recovery power plant of the present embodiment, the feed water supplied from the condenser 53 and the low pressure stage flasher 42 by the feed water pump 54 is heated by the economizer 37 of the SC boiler 30 and the steam drum 36 and the high pressure stage. Distributed to the flasher 41. The hot water supplied to the steam drum 36 is heated by the evaporator 35 and returns to the steam drum 36 to generate gas-liquid separation to generate steam. The generated saturated steam becomes high-pressure steam in the superheater 33, and the steam turbine 51. To the high pressure stage.

The hot water supplied to the high pressure stage flasher 41 is separated into steam and hot water by the high pressure stage flasher 41, and the steam is supplied to the intermediate pressure stage of the steam turbine 51. Hot water is supplied to the low-pressure stage flasher 42, but a part of the hot water is taken out by the booster pump 43 in the middle of the piping and supplied to the economizer 17 of the SM boiler 10. The hot water supplied to the economizer 17 is heated by the economizer 17 and then supplied to the steam drum 16, and the surplus is distributed to the high-pressure stage flasher 41.
The hot water supplied to the steam drum 16 of the SM boiler 10 becomes high-pressure steam by the evaporator 15 and the heater 13 and is supplied to the high-pressure stage of the steam turbine 51 together with the high-pressure steam supplied from the SC boiler 30. The

In addition, surplus hot water supplied from the economizer 17 of the SM boiler 10 is supplied to the high-pressure stage flasher 41 together with surplus hot water supplied from the economizer 37 of the SC boiler 30. Increase the amount of pressurized steam and hot water.
The hot water supplied to the low-pressure stage flasher 42 is separated into low-pressure steam and hot water, and the low-pressure steam is supplied to the low-pressure stage of the steam turbine 51 to increase the generated power in the generator 52.

  Also in the waste heat recovery power plant of this embodiment, the heat energy supplied to the steam turbine 51 can be increased by the amount of waste heat recovered in the SM boiler 10, so the power generation amount increases. However, since there is a restriction that the exhaust gas temperature at the outlet of the SM boiler 10 must exceed the acid dew point, the hot water heated by using a part of the waste heat recovered by the SM boiler 10 is received and used. Thus, a larger amount of high-pressure steam that can be used in the steam turbine 51 is generated.

  However, instead of directly receiving the hot water from the SC boiler 30 to the steam drum 16, the hot water of the high-pressure stage flasher 41 is received via the economizer 17, and steam of the hot water heated by the economizer 17 is used. The surplus portion excluding the amount supplied to the drum 16 and converted into high-pressure steam is returned to the high-pressure stage flasher 41 and used to generate medium-pressure steam.

  Also in the waste heat recovery power plant of the second embodiment, the amount of high-pressure steam generated by the SM boiler 10 is increased by a part of the amount of heat recovered by the SC boiler 30 for use in obtaining high-pressure steam by the SM boiler 10. It will be. Further, in addition to supplying low-pressure steam generated by the low-pressure stage flasher 42 of the two-stage flasher 40 to the low-pressure stage of the steam turbine 51, the SC boiler 30 and the SM boiler 10 are added to the high-pressure stage flasher 41 of the two-stage flasher 40. The steam turbine 51 is supplied with a portion of the hot water to generate steam suitable for the intermediate pressure stage of the steam turbine 51 and inject it into the intermediate pressure stage of the steam turbine 51, thereby enhancing the output of the steam turbine 51 and generating power. The power generated by the device 50 is reinforced.

For example, gas-liquid separation is performed while maintaining the pressure of the high-pressure stage flasher 41 at an intermediate-pressure stage pressure corresponding to the saturation temperature of 144 ° C., and a part of the generated hot water is supplied to the economizer 17 of the SM boiler 10. Thus, the exhaust gas temperature at the outlet of the SM boiler 10 can be maintained at about 160 ° C., which is 20 to 40 ° C. higher than the acid dew point.
Therefore, droplet sulfation due to condensation of sulfuric anhydride or sulfurous acid gas contained in the exhaust gas can be suppressed, and corrosion of the heat transfer surface of the waste heat boiler 11 and the exhaust system equipment can be prevented.

  The waste heat recovery power plant of the present embodiment is provided with an independent water supply system for each of the SM boiler 10 and the SC boiler 30 and the SM boiler 10 is equipped with the economizer 17. Since more waste heat can be recovered, it is suitable when the ratio of the sintering machine 1 to the entire waste heat that can be used by the sintering machine 1 and the sintering cooler 2 is large.

  The waste heat recovery power plant for sintering equipment of the present invention is applied to a sintering equipment for producing sintered ore required for iron making, thereby recovering waste heat generated in the sintering machine as electric power to save energy. Can be achieved.

DESCRIPTION OF SYMBOLS 1 Sintering machine 2 Sinter ore cooler 3, 4 Dust collector 5, 6 Chimney 7, 8, 9 Ventilation machine 10 Sintering machine waste heat boiler (SM boiler)
DESCRIPTION OF SYMBOLS 11 Boiler main body 13 Superheater 15 Evaporator 16 Steam drum 17 Carbon-saving device 30 Sinter cooler waste heat boiler (SC boiler)
31 boiler body 33 superheater 35 evaporator 36 steam drum 37 economizer 40 two-stage flasher 41 high-pressure stage flasher 42 low-pressure stage flasher 43 booster pump 50 power generator 51 steam turbine 52 generator 53 condenser 54 feed pump

Claims (3)

A waste heat recovery power plant applied to a sintering facility equipped with a sintering machine and a sintered ore cooler,
A sintered ore cooler waste heat boiler that includes a first evaporator, a first economizer, a first superheater, and a first steam drum, and that introduces exhaust gas from the sintered ore cooler to generate hot water and steam; ,
Includes a second evaporator and a second superheater second steam drum, a sintering machine waste heat boiler to generate steam by introducing Atsushi Ko exhaust gas generated in sintering completion region of the sintering machine,
A multi-stage steam turbine combined with a generator;
A two-stage flasher for supplying the steam of the first stage flasher to the intermediate pressure stage of the multistage steam turbine and the steam of the second stage flasher to the low pressure stage of the multistage steam turbine;
The condensate of the multistage steam turbine and the return hot water of the two-stage flasher are heated by the first economizer, and the heated hot water is heated to the two-stage flasher, the second steam drum, and the second Distribute to one steam drum,
Supplying steam generated by the first evaporator and the first superheater and steam generated by the second evaporator and the second superheater to a high-pressure stage of the multistage steam turbine;
When maintaining the exhaust gas in the exhaust gas outlet of the sintering machine waste heat boiler to a temperature above the acid dew point, low temperature of the exhaust gas generated in the ignition zone of the sintering machine and exhaust gas of the sintering machine waste heat boiler merges A waste heat recovery power plant for sintering equipment, characterized by maintaining the exhaust gas at a temperature higher than the water dew point. A waste heat recovery power plant applied to a sintering facility equipped with a sintering machine and a sintered ore cooler,
A sinter cooler waste heat boiler that includes a first evaporator, a first superheater, a first economizer, and a first steam drum, and introduces exhaust gas from the sinter cooler to generate hot water and steam;
Comprising a second evaporator and a second superheater and second economiser the second steam drum, sintering machine by introducing a Atsushi Ko exhaust gas generated in sintering completion region of the sintering machine to generate steam Waste heat boiler,
A multi-stage steam turbine combined with a generator;
A two-stage flasher for supplying the steam of the first stage flasher to the intermediate pressure stage of the multistage steam turbine and the steam of the second stage flasher to the low pressure stage of the multistage steam turbine;
The condensate of the multi-stage steam turbine and the return hot water of the second stage flasher are heated by the first economizer, and the heated hot water is distributed to the first stage flasher and the first steam drum. ,
The hot water of the first stage flasher is heated by the second economizer and distributed to the first stage flasher and the second evaporation drum,
Supplying steam generated by the first evaporator and the first superheater and steam generated by the second evaporator and the second superheater to a high-pressure stage of the multistage steam turbine;
When maintaining the exhaust gas in the exhaust gas outlet of the sintering machine waste heat boiler to a temperature above the acid dew point, low temperature of the exhaust gas generated in the ignition zone of the sintering machine and exhaust gas of the sintering machine waste heat boiler merges A waste heat recovery power plant for sintering equipment, characterized by maintaining the exhaust gas at a temperature higher than the water dew point. The exhaust gas temperature at the exhaust gas outlet of the sintering machine waste heat boiler is maintained at 160 ° C. or higher, and the exhaust gas temperature at the place where the exhaust gas from the sintering machine waste heat boiler and the exhaust gas from the sintering machine merge is maintained at 100 ° C. or higher. The waste heat recovery power plant for sintering equipment according to claim 1 or 2, wherein the power plant is operated as described above.

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