CN102330968A - Two-stage flue gas heat exchanger system applied to thermal power plant - Google Patents
Two-stage flue gas heat exchanger system applied to thermal power plant Download PDFInfo
- Publication number
- CN102330968A CN102330968A CN2010102248592A CN201010224859A CN102330968A CN 102330968 A CN102330968 A CN 102330968A CN 2010102248592 A CN2010102248592 A CN 2010102248592A CN 201010224859 A CN201010224859 A CN 201010224859A CN 102330968 A CN102330968 A CN 102330968A
- Authority
- CN
- China
- Prior art keywords
- flue gas
- heat exchanger
- stage
- condensed water
- gas heat
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 239000003546 flue gas Substances 0.000 title claims abstract description 561
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 559
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 256
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 78
- 230000023556 desulfurization Effects 0.000 claims abstract description 78
- 239000000428 dust Substances 0.000 claims abstract description 62
- 239000002918 waste heat Substances 0.000 claims abstract description 48
- 238000011084 recovery Methods 0.000 claims description 18
- 238000000034 method Methods 0.000 claims description 16
- 238000010438 heat treatment Methods 0.000 claims description 14
- 239000002253 acid Substances 0.000 claims description 9
- 238000004378 air conditioning Methods 0.000 claims description 5
- 238000009423 ventilation Methods 0.000 claims description 5
- 239000007789 gas Substances 0.000 claims description 4
- 239000000779 smoke Substances 0.000 description 28
- 239000003245 coal Substances 0.000 description 27
- 239000007788 liquid Substances 0.000 description 24
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 16
- 230000008901 benefit Effects 0.000 description 16
- 238000010521 absorption reaction Methods 0.000 description 15
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 14
- 238000009835 boiling Methods 0.000 description 10
- 239000002002 slurry Substances 0.000 description 8
- 238000002485 combustion reaction Methods 0.000 description 7
- 230000000630 rising effect Effects 0.000 description 7
- 230000000875 corresponding effect Effects 0.000 description 6
- 230000007797 corrosion Effects 0.000 description 6
- 238000005260 corrosion Methods 0.000 description 6
- 230000000694 effects Effects 0.000 description 6
- 238000005265 energy consumption Methods 0.000 description 6
- 238000000605 extraction Methods 0.000 description 6
- 238000000746 purification Methods 0.000 description 6
- 230000009467 reduction Effects 0.000 description 5
- 238000009833 condensation Methods 0.000 description 4
- 230000005494 condensation Effects 0.000 description 4
- 230000003009 desulfurizing effect Effects 0.000 description 4
- 239000003344 environmental pollutant Substances 0.000 description 4
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 description 4
- 231100000719 pollutant Toxicity 0.000 description 4
- 230000008569 process Effects 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 3
- 230000008020 evaporation Effects 0.000 description 3
- 238000010248 power generation Methods 0.000 description 3
- 238000005507 spraying Methods 0.000 description 3
- 230000009471 action Effects 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 239000000498 cooling water Substances 0.000 description 2
- 230000002596 correlated effect Effects 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 230000001172 regenerating effect Effects 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 238000010276 construction Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 239000003077 lignite Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
Images
Landscapes
- Chimneys And Flues (AREA)
Abstract
The invention provides a two-stage flue gas heat exchanger system applied to a thermal power plant, which comprises a boiler unit for exhausting flue gas, a flue gas waste heat utilizing unit, a flue gas dust removing unit and a flue gas desulfurization unit, wherein the flue gas waste heat utilizing unit comprises a preheater, a flue gas dust removing unit, a first-stage flue gas heat exchanger arranged at an inlet of the flue gas dust removing unit and a second-stage flue gas heat exchanger arranged at an inlet of the flue gas desulfurization unit; the first-stage flue gas heat exchanger and the second-stage flue gas heat exchanger are respectively flue gas-condensed water heat exchangers provided with flue gas sides for radiating heat and condensed water sides for absorbing heat; a water source at each condensed water side is condensed water in a condensed water system of a steam turbine; and the first-stage flue gas heat exchanger is connected with the second-stage flue gas heat exchanger according to one of modes: the flue gas side of the first-stage flue gas heat exchanger is connected with the flue gas side of the second-stage flue gas heat exchanger in series; the condensed water side of the first-stage flue gas heat exchanger is connected with the condensed water side of the second-stage flue gas heat exchanger in parallel; and the flue gas side and the condensed water side of the first-stage flue gas heat exchanger are respectively connected with the flue gas side and the condensed water side of the second-stage flue gas heat exchanger in series.
Description
Technical Field
The invention relates to environment-friendly energy-saving equipment, in particular to a flue gas waste heat utilization system which is applied to a thermal power plant and is used for reducing smoke dust emission, improving desulfurization efficiency and saving water consumption and comprehensively optimizing flue gas.
Background
With the development of national economy, the demand of society for electric power is continuously increasing. For emerging developing countries, such as china, in which industrialization and rapid economic development are underway, the consumption of electric power and the installed capacity of power plants are rapidly increasing. In China, the fuel of a power plant is mainly coal and reaches over 70 percent in recent decades due to the limitation of the storage variety and the storage capacity of primary energy, and the trend cannot be fundamentally changed in the foreseeable future. Although the coal-fired thermal power plant has the advantages of low cost, wide fuel source and the like for China, the coal-fired thermal power plant has the defects of low efficiency, high pollutant emission and the like. Since pollutants discharged into the atmosphere are basically derived from the combustion of coal, the discharge amount of pollutants is positively correlated with the coal consumption of a thermal power plant, and is also correlated with the flue gas purification efficiency of the flue gas purification equipment. Therefore, the method is a promising technology aiming at optimizing the flue gas system of the thermal power plant, reducing the coal consumption of the thermal power plant and simultaneously improving the purification efficiency of the flue gas purification equipment so as to realize energy conservation and simultaneously reduce the emission of pollutants from the thermal power plant to the atmosphere.
Generally, the following three methods can be employed to reduce coal consumption in a thermal power plant. And (I) increasing the pressure and temperature of the steam. After the pressure and the temperature of the steam are improved, the efficiency of the steam turbine is improved, the heat consumption is reduced, the efficiency of the whole thermal power generation system can be improved, and the coal consumption is reduced. At present, the steam pressure and the temperature of a mainstream thermal power generating unit are increased from subcritical parameters to supercritical parameters, and further increased to supercritical parameters. At present, a continuous technical research is being carried out at home and abroad for further improving the steam temperature. However, when the temperature and the pressure of the steam are increased by one step, the boiler and the steam turbine need to adopt materials with higher heat strength and higher corrosion resistance, and the construction and maintenance cost of the unit is greatly increased. And (II) reducing the steam exhaust parameters of the steam turbine. After the exhaust steam parameters of the steam turbine are reduced, the efficiency of the steam turbine can be improved, and the heat consumption of the steam turbine is reduced. The reduction of the steam discharge parameters of the steam turbine requires the reduction of the temperature of the circulating cooling water of the steam turbine, and the temperature of the circulating cooling water is changed within a certain range due to the limitation of the geographical position and the climate condition of the power plant, so the reduction range of the steam discharge parameters of the steam turbine is limited. For the same region, the steam discharge parameters of the steam turbine are fixed. And (III) reducing the heat loss of the boiler flue gas. The temperature of the flue gas generated after the boiler is combusted is generally between 110 and 170 ℃ according to different boiler forms and different types of fire coal. In general, the boiler flue gas is directly discharged to the atmosphere after being purified, and the temperature of the discharged flue gas is hardly changed, namely, the heat in the flue gas is directly discharged to the atmosphere without utilization. In the wet flue gas desulfurization process, the temperature of the flue gas is reduced to 40-50 ℃ in a desulfurization absorption tower under the spraying action of the slurry of the desulfurizing agent, and the heat of the flue gas is taken away by the slurry in the process, so that the water in the slurry is evaporated. The higher the flue gas temperature, the greater the evaporation of water from the slurry, and the greater the water consumption of the power plant. Because some power plants are required to be in environment protection, the temperature of the flue gas discharged into the atmosphere is not lower than 72-80 ℃, and the flue gas at the outlet of the desulfurization absorption tower needs to be heated to be higher than the temperature, so a flue gas-flue gas heat exchanger or a flue gas-water-flue gas heat exchanger is adopted to heat the flue gas with higher temperature discharged from a boiler to the flue gas with lower temperature discharged from the desulfurization absorption tower, and the heat of the flue gas discharged from the boiler is still not recycled because the heated flue gas is still discharged into the atmosphere.
Therefore, the utilization of the waste heat of the boiler flue gas is an effective way for reducing the coal consumption of the thermal power plant. The utilization of the waste heat of the boiler flue gas has a plurality of designs and practices at home and abroad, and the flue gas heat exchanger is adopted, and the heat in the flue gas is replaced to other media by the heat exchanger for utilization. The flue gas heat exchanger is called as a low-temperature economizer, a low-pressure economizer, a flue gas cooler, a flue gas water heat exchanger and the like, and the actual names of the flue gas heat exchanger are the same or similar
Specifically, the prior art flue gas heat exchanger is arranged as follows:
(1) the flue gas heat exchanger is arranged at the tail part of the boiler, and condensed water is adopted to absorb the waste heat of the flue gas. For example, the exhaust gas temperature of a certain power plant boiler in China is high, in order to reduce the exhaust gas temperature and improve the operation economy of a unit, a low-temperature economizer is additionally arranged at the outlet of an air preheater at the tail part of the boiler, and condensed water is adopted to absorb the waste heat of the exhaust gas, which is shown in the attached drawing 1. When the boiler unit is modified in order to reduce the smoke discharge loss in the former Soviet Union, a low-temperature economizer is arranged at the lower part of a convection shaft of the boiler, and heat supply network water is adopted to absorb the waste heat of smoke.
(2) The flue gas heat exchanger is arranged in front of the desulfurization absorption tower, and condensed water is adopted to absorb the waste heat of the flue gas. A2 x 800MW lignite power generation unit of a German Schwarze Pumpe power plant is additionally provided with a flue gas cooler between an electrostatic dust collector and a flue gas desulfurization tower, and condensed water is adopted to absorb the waste heat of flue gas, which is shown in figure 2.
In summary, the existing solutions of these flue gas heat exchangers all use a primary flue gas-water heat exchanger or a flue gas-air heat exchanger, which mainly functions to recover the flue gas waste heat and reduce the coal consumption of the generator set, so that the functions are relatively single.
Those skilled in the art are devoted to obtain an improved device of the above flue gas heat exchanger arrangement, which has the functions of reducing smoke emission, reducing sulfur dioxide emission, saving water for a desulfurization device, preventing low-temperature corrosion of an air preheater, reducing power consumption of a fan, saving coal consumption of a unit and the like.
In summary, there is a need in the art for an improved flue gas waste heat utilization system of a thermal power plant, which has multiple functions of reducing smoke emission, reducing sulfur dioxide emission, saving water for a desulfurization device, preventing low-temperature corrosion of an air preheater, reducing power consumption of a fan, and saving coal consumption of a unit.
Disclosure of Invention
The first purpose of the invention is to provide an improved device of the above smoke heat exchanger arrangement, which has the functions of reducing smoke emission, reducing sulfur dioxide emission, saving water for a desulfurization device, preventing low-temperature corrosion of an air preheater, reducing power consumption of a fan, saving coal consumption of a unit and the like.
The second purpose of the invention is to provide a method for utilizing the residual heat of the flue gas by using the improved device of the flue gas heat exchanger arrangement, which has the functions of reducing smoke emission, reducing sulfur dioxide emission, saving water for desulfurization equipment, preventing low-temperature corrosion of an air preheater, reducing power consumption of a fan, saving coal consumption of a unit and the like.
The third objective of the present invention is to provide a thermal power plant system containing the improved device of the above flue gas heat exchanger arrangement, which has the functions of reducing smoke emission, reducing sulfur dioxide emission, saving water for desulfurization equipment, preventing low-temperature corrosion of air preheater, reducing power consumption of blower, and saving coal consumption of unit.
The invention provides a two-stage flue gas heat exchanger system applied to a thermal power plant, which comprises a boiler unit for discharging flue gas, a flue gas waste heat utilization unit, a flue gas dedusting unit and a flue gas desulfurization unit, wherein the flue gas waste heat utilization unit comprises:
-a preheater;
-a first stage flue gas heat exchanger arranged at the inlet of the flue gas dust removal unit, and a second stage flue gas heat exchanger arranged at the inlet of the flue gas desulfurization unit;
wherein,
the first-stage flue gas heat exchanger and the second-stage flue gas heat exchanger are both flue gas-condensed water heat exchangers provided with a heat-releasing flue gas side and a heat-absorbing condensed water side; the water source at the condensed water side is condensed water in a turbine condensed water system; and is
The first-stage flue gas heat exchanger and the second-stage flue gas heat exchanger are connected in one of the following modes:
the flue gas sides of the two are connected in series, and the condensed water sides of the two are connected in parallel; or
The flue gas side and the condensate side of both are connected in series.
In a preferred embodiment, an induced draft fan and an optional desulfurization booster fan are arranged at the downstream of the flue gas dust removal unit, so that flue gas enters a subsequent second-stage flue gas heat exchanger after the pressure of the induced draft fan and the desulfurization booster fan is increased.
In an embodiment of the invention, the water side water sources of the first stage flue gas heat exchanger and the second stage flue gas heat exchanger further comprise adjacent turbine system condensed water, heat supply network water, heating ventilation and air conditioning system water, power plants and other domestic water.
In one embodiment of the invention, the condensate is derived from the outlet of a low pressure heater of a stage or a collection of low pressure heater outlets of stages of a turbine condensate system.
Specifically, the condensed water returns to the inlet or the outlet of a certain stage of low-pressure heater after absorbing heat through the flue gas heat exchanger.
In a preferred example, the turbine condensate system is further provided with a condensate booster pump.
In a preferred embodiment, the flue gas heat exchanger and one or more stages of low-pressure heaters are connected in series or in parallel or in a series-parallel relationship in the condensed water flow.
In a preferred embodiment, the condensed water absorbs heat through the first-stage flue gas heat exchanger and then returns to the inlet or the outlet of a certain-stage low-pressure heater, that is, the first-stage flue gas heat exchanger and a certain-stage or several-stage low-pressure heater are in series or parallel connection or in series or parallel connection.
In one embodiment of the present invention, the first stage flue gas heat exchanger or the second stage flue gas heat exchanger is a surface heat exchanger.
In a specific embodiment of the present invention, the first stage flue gas heat exchanger or the second stage flue gas heat exchanger is a heat pipe type heat exchanger.
In a specific embodiment of the present invention, the first stage flue gas heat exchanger or the second stage flue gas heat exchanger adopts an indirect heat exchanger with an intermediate carrier.
In a preferred embodiment, the heating medium of the intermediate carrier is in a liquid state. The liquid heating medium is selected from water or other low boiling point liquid, preferably ethylene glycol.
In one embodiment of the invention, each stage of heat exchanger is a heat exchanger, or a plurality of heat exchangers connected in parallel
The second aspect of the invention provides a method for recovering flue gas waste heat by using the two-stage flue gas heat exchanger system, which can reduce the smoke dust emission concentration, water consumption and power consumption of an induced draft fan and a booster fan, and comprises the following steps:
the method comprises the following steps of (1) enabling flue gas generated by a boiler unit to pass through a preheater in a flue gas heat exchanger system to obtain preheated flue gas at the temperature of 110-170 ℃;
the preheated flue gas is subjected to waste heat recovery in a first-stage flue gas heat exchanger, so that the temperature of the preheated flue gas is reduced to be 5-10 ℃ above the acid dew point temperature of the flue gas, and first-stage flue gas subjected to waste heat recovery is obtained; meanwhile, the specific resistance of the flue gas is reduced, the dust removal efficiency is improved, the smoke emission concentration is reduced, and the submitted flow of the flue gas is reduced, so that the power consumption of an induced draft fan and a booster fan is reduced;
the temperature of the primary flue gas subjected to waste heat recovery is reduced to be 20-25 ℃ above the dew point temperature of water or the required optimal flue gas temperature after passing through a secondary flue gas heat exchanger, so that secondary flue gas subjected to waste heat recovery is obtained; meanwhile, the water consumption of a desulfurization system is reduced;
and the flue gas subjected to waste heat recovery in the second stage enters a flue gas desulfurization unit.
Specifically, the optimal flue gas temperature is determined according to the comprehensive economic technology of the manufacturing cost of the flue gas heat exchanger, the occupied arrangement space of the flue gas heat exchanger and the saved coal consumption benefit of the power plant.
In a preferred embodiment, the flue gas subjected to waste heat recovery at the primary stage enters a flue gas dust removal unit, and enters a secondary flue gas heat exchanger after the pressure of the flue gas is increased by an induced draft fan and an optional desulfurization booster fan.
The invention also provides a thermal power plant system containing the flue gas waste heat utilization system.
Drawings
FIG. 1 is a layout of a flue gas heat exchanger in the prior art, which is arranged at the tail of a boiler and adopts condensed water to absorb the waste heat of flue gas;
FIG. 2 is a prior art arrangement of a flue gas heat exchanger, which is arranged before a desulfurization absorption tower and absorbs flue gas waste heat by using condensed water;
FIG. 3 is an alternate embodiment of the two stage flue gas heat exchanger system of the present invention;
FIG. 4 is an alternate embodiment of the two stage flue gas heat exchanger system of the present invention;
FIG. 5 is an alternate embodiment of the two stage flue gas heat exchanger system of the present invention;
FIG. 6 is an alternate embodiment of the two stage flue gas heat exchanger system of the present invention;
FIG. 7 is an alternate embodiment of the two stage flue gas heat exchanger system of the present invention;
FIG. 8 is an alternate embodiment of the two stage flue gas heat exchanger system of the present invention;
FIG. 9 is an alternate embodiment of the two stage flue gas heat exchanger system of the present invention;
FIG. 10 is an alternative embodiment of the two-stage flue gas heat exchanger system of the present invention.
Detailed Description
Through extensive and intensive research, the designer of the invention obtains a flue gas waste heat utilization system which is applied to a thermal power plant and is used for reducing smoke dust emission, improving desulfurization efficiency and saving water consumption and comprehensively optimizing the flue gas by improving a preparation process. The present invention has been completed based on this finding.
The technical concept of the invention is as follows:
the invention adopts a two-stage boiler flue gas heat exchanger and a system thereof, and uses condensed water in a turbine condensed water system to cool boiler flue gas. After the system is adopted, the coal consumption of the thermal power generating unit can be reduced, the efficiency of flue gas purification equipment, namely an electrostatic dust collector, is improved, the discharge amount of smoke dust is reduced, the power consumption of an induced draft fan and a booster fan of a flue gas system is reduced, the water consumption of the flue gas purification equipment, namely a flue gas desulfurization tower is reduced, the efficiency of the flue gas desulfurization tower is improved, and the discharge amount of sulfur dioxide is reduced.
The terminology of the present invention is known to those skilled in the art unless otherwise specified. Specifically, for example, see "thermal power plant" of power press of China.
Herein, the "boiler unit" mainly comprises a boiler device. The boiler device is not particularly limited as long as it does not impose a limitation on the object of the present invention, and is known to those skilled in the art. The invention can adopt pi-type boiler, tower boiler, etc., all of which are in the protection scope of the invention.
Herein, the "preheater" is not particularly limited as long as it does not impose limitation on the object of the present invention, and is known to those skilled in the art. Tubular preheaters, rotary preheaters and the like can be adopted and are all within the protection scope of the invention.
Herein, the "flue gas dust removal unit" refers to a device for capturing dust in flue gas. Preferably, a design is used which controls the flow rate and optimizes the distribution of the flue gas flow field. As long as it does not limit the object of the present invention, it is known to those skilled in the art. The electrostatic dust collector, the cloth bag flue gas dust removal unit, the electric bag flue gas dust removal unit, the water film flue gas dust removal unit and the like can be adopted and are all within the protection scope of the invention.
Herein, the flue gas desulfurization unit includes various conventional desulfurization apparatuses in the art.
In this context, each stage of flue gas heat exchanger is a heat exchanger, or a plurality of heat exchangers connected in parallel.
Herein, the induced draft fan is not particularly limited as long as it does not limit the object of the present invention, and is known to those skilled in the art.
Herein, the desulfurization booster fan is not particularly limited as long as it does not limit the object of the present invention, and is known to those skilled in the art.
Herein, the flue gas heat exchanger includes a flue gas and air direct heat exchanger or an indirect heat exchanger with an intermediate heating medium. Preferably a tubular heat exchanger or a rotary heat exchanger. Preferably a liquid heating medium is used. The liquid heating medium comprises water or other liquid with low boiling point, preferably glycol. The heat medium is maintained in flow between the flue gas side/air side and heat medium side heat exchangers by a heat medium circulation pump. When a liquid heating medium such as a liquid with a low boiling point is used, it is preferable to provide a gas-liquid condensation separation device on the circulation circuit, and the circulation pump is provided downstream of the device.
The turbine condensate system may be part of a turbine regenerative system, but is not limited thereto, and may be, for example, adjacent turbine condensate, heat supply network water, heating, ventilation, air conditioning system water, power plants, and other domestic water. The condensate pump in the turbine condensate system overcomes the condensate resistance of the flue gas heat exchanger and the condensate pipeline at the inlet and the outlet of the flue gas heat exchanger, or overcomes the condensate resistance of the flue gas heat exchanger and the condensate pipeline at the inlet and the outlet of the flue gas heat exchanger by the condensate booster pump. The range of boost pump boost required is known to those skilled in the art. Which may contain low pressure heaters for each stage. The meaning of the low-pressure heater is known to the person skilled in the art.
Herein, the steam turbine system condensate water, the heat supply network water, the heating ventilation air conditioning system water, the power plant and other domestic water of the adjacent machine are not particularly limited as long as the object of the present invention is not limited, and are known to those skilled in the art.
Various aspects of the invention are described in detail below, with the terminology of the invention being known to those skilled in the art unless otherwise specified. Specifically, for example, see "thermal power plant" of power press of China.
Two-stage flue gas heat exchanger system applied to thermal power plant
The invention provides a two-stage flue gas heat exchanger system applied to a thermal power plant, which comprises a boiler unit (100) for discharging flue gas, a flue gas waste heat utilization unit (200), a flue gas dust removal unit (300) and a flue gas desulfurization unit (400), wherein the flue gas waste heat utilization unit (200) comprises:
-a preheater (2);
-a first stage flue gas heat exchanger (31) arranged at the inlet of the flue gas dust removal unit (300), and a second stage flue gas heat exchanger (32) arranged at the inlet of the flue gas desulfurization unit (400);
wherein,
the first-stage flue gas heat exchanger (31) and the second-stage flue gas heat exchanger (32) are both flue gas-condensed water heat exchangers provided with a heat-releasing flue gas side and a heat-absorbing condensed water side; the water source at the condensed water side is condensed water in a turbine condensed water system; and is
The first-stage flue gas heat exchanger (31) and the second-stage flue gas heat exchanger (32) are connected in one of the following ways:
the flue gas sides of the two are connected in series, and the condensed water sides of the two are connected in parallel; or
The flue gas side and the condensate side of both are connected in series.
In the invention, the two stages of flue gas heat exchangers are connected in series in the flue gas flow and are connected in parallel in the condensed water flow.
Or the two-stage flue gas heat exchangers are connected in series in the flue gas flow and are also connected in series in the condensed water flow. For a two-stage flue gas heat exchanger, the flow direction of flue gas and condensed water is concurrent flow.
Or the two-stage flue gas heat exchangers are connected in series in the flue gas flow and are also connected in series in the condensed water flow. For a two-stage flue gas heat exchanger, the flow direction of flue gas and condensed water is countercurrent.
In one embodiment of the invention, the first stage flue gas heat exchanger (31) or the second stage flue gas heat exchanger (32) adopts a surface type heat exchanger.
In one embodiment of the invention, the first-stage flue gas heat exchanger (31) or the second-stage flue gas heat exchanger (32) adopts a heat pipe type heat exchanger.
In one embodiment of the invention, the first stage flue gas heat exchanger (31) or the second stage flue gas heat exchanger (32) adopts an indirect heat exchanger with an intermediate carrier.
In a preferred embodiment, the heating medium of the intermediate carrier is in a liquid state. The liquid heating medium is selected from water or other low boiling point liquid, preferably ethylene glycol.
In one embodiment of the invention, two stages of flue gas heat exchangers are adopted and are respectively arranged at the inlet of the dust remover and the inlet of the desulfurization absorption tower. Each stage of flue gas heat exchanger is a heat exchanger or a plurality of heat exchangers connected in parallel. Each stage of heat exchanger is a heat exchanger or a plurality of heat exchangers connected in parallel
In a preferred embodiment, the downstream of the flue gas dust removal unit (300) is provided with an induced draft fan (5) and an optional desulfurization booster fan (6), so that flue gas enters a subsequent second-stage flue gas heat exchanger (32) after the pressure of the induced draft fan (5) and the desulfurization booster fan (6) is increased.
In one embodiment of the invention, the water side water sources of the first stage flue gas heat exchanger (31) and the second stage flue gas heat exchanger (32) further comprise adjacent turbine system condensed water, heat supply network water, water for heating ventilation and air conditioning systems, power plants and other domestic water.
In one embodiment of the invention, the condensate is derived from the outlet of a low pressure heater of a stage or a collection of low pressure heater outlets of stages of a turbine condensate system.
Specifically, the condensed water returns to the inlet or the outlet of a certain stage of low-pressure heater after absorbing heat through the flue gas heat exchanger.
In a preferred example, the turbine condensate system is further provided with a condensate booster pump.
In a preferred embodiment, the condensed water of the flue gas heat exchanger comes from the outlet of a certain level of low-pressure heater or the outlets of a plurality of levels of low-pressure heaters and is collected, that is, the flue gas heat exchanger and the certain level or the plurality of levels of low-pressure heaters are in series or parallel connection or in a series-parallel connection relationship in the flow of the condensed water.
In a preferred embodiment, the condensed water absorbs heat through the first-stage flue gas heat exchanger and then returns to the inlet or the outlet of a certain-stage low-pressure heater, that is, the first-stage flue gas heat exchanger and a certain-stage or several-stage low-pressure heater are in series or parallel connection or in series or parallel connection.
More preferably, the condensate water resistance of the flue gas heat exchanger and the condensate water pipeline at the inlet and the outlet of the flue gas heat exchanger is overcome by a condensate water pump in a condensate water system of the steam turbine.
Or the condensate booster pump overcomes the condensate resistance of the flue gas heat exchanger and the condensate pipeline at the inlet and the outlet of the flue gas heat exchanger.
Method for recovering flue gas waste heat by two-stage flue gas heat exchanger system
The second aspect of the invention provides a method for recovering flue gas waste heat by using the two-stage flue gas heat exchanger system, which can reduce the smoke dust emission concentration, water consumption and power consumption of an induced draft fan and a booster fan, and comprises the following steps:
enabling the flue gas generated by the boiler unit (100) to pass through a preheater (2) in the flue gas waste heat utilization unit (200) to obtain preheated flue gas at the temperature of 110-170 ℃;
the preheated flue gas is subjected to waste heat recovery in a first-stage flue gas heat exchanger (31), so that the temperature of the preheated flue gas is reduced to be 5-10 ℃ above the acid dew point temperature of the flue gas, and first-stage flue gas subjected to waste heat recovery is obtained; meanwhile, the specific resistance of the flue gas is reduced, the dust removal efficiency is improved, the smoke emission concentration is reduced, and the submitted flow of the flue gas is reduced, so that the power consumption of an induced draft fan and a booster fan is reduced;
the temperature of the primary flue gas after waste heat recovery is reduced to be 20-25 ℃ above the dew point temperature of water or the required optimal flue gas temperature after passing through a secondary flue gas heat exchanger (32), so that secondary flue gas after waste heat recovery is obtained; meanwhile, the water consumption of a desulfurization system is reduced;
and the flue gas subjected to waste heat recovery in the second stage enters a flue gas desulfurization unit.
Specifically, the optimal flue gas temperature is determined according to the comprehensive economic technology of the manufacturing cost of the flue gas heat exchanger, the occupied arrangement space of the flue gas heat exchanger and the saved coal consumption benefit of the power plant.
In a preferred embodiment, the primary flue gas after waste heat recovery enters a flue gas dust removal unit (300), and enters a secondary flue gas heat exchanger (32) after the pressure of the flue gas is increased by an induced draft fan (5) and an optional desulfurization booster fan (6).
Thermal power plant system of flue gas waste heat utilization system
The invention also provides a thermal power plant system containing the flue gas waste heat utilization system.
The invention has the advantages that:
the two-stage flue gas heat exchanger is respectively arranged at the inlet of the dust remover and the inlet of the desulfurization absorption tower, and the condensed water in the turbine regenerative system is adopted to absorb the heat in the flue gas.
Unless otherwise specified, various apparatuses of the present invention are commercially available.
Other aspects of the invention will be apparent to those skilled in the art in view of the disclosure herein.
The invention will be further illustrated with reference to the following specific examples. It should be understood that these examples are for illustrative purposes only and are not intended to limit the scope of the present invention. The experimental procedures, in which specific conditions are not specified, in the following examples are generally carried out according to conventional conditions or according to conditions recommended by the manufacturers. Unless otherwise indicated, all parts are parts by weight, all percentages are percentages by weight, and the molecular weight of the polymer is the number average molecular weight.
Unless defined or stated otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs. In addition, any methods and materials similar or equivalent to those described herein can be used in the methods of the present invention.
The flue gas heat exchanger system of the invention is further described with reference to the accompanying drawings, wherein the flue gas energy-saving emission-reducing water-saving system is composed of the following main parts:
(1) boiler 100
(2) Air preheater 2
(3) First stage flue gas heat exchanger 31
(4) Dust remover (flue gas dust removal unit 300)
(5) Draught fan 5
(6) Booster fan 6
(7) Second stage flue gas heat exchanger 32
(8) Desulfurizing absorption tower 400 (flue gas desulfurizing unit)
(9) Chimney
(10) Low-pressure heater 7 (short for 'Low heating')
(11) Condensate booster pump 8
(12) Circulating pump 9
(13) Condenser 10
(14) Condenser 11
(15) Steam turbine low pressure cylinder 12
(16) Generator 13
(17) Condensate pump 14
(18) Flash tank 15
Example 1 (corresponding to FIGS. 3 and 4)
The flue gas generated by the combustion of the boiler 100 passes through the air preheater 2, and the temperature is generally between 110 ℃ and 170 ℃ according to the type of the boiler and the type of the fire coal. The temperature of the flue gas is reduced to about 10 ℃ above the acid dew point temperature of the flue gas after passing through the first-stage flue gas heat exchanger 31. The first-stage flue gas heat exchanger 31 uses flue gas-condensed water as a heat exchange medium, and the flue gas side releases heat and the condensed water side absorbs heat. The flue gas is derived from boiler flue gas at the outlet of the air preheater. The condensed water is from a turbine condensed water system, namely from the outlet of a certain level of low-pressure heater 7 or the outlets of a plurality of levels of low-pressure heaters 7 and gathered, the condensed water returns to the inlet or the outlet of the certain level of low-pressure heater 7 after absorbing heat through the first level of flue gas heat exchanger 31, namely the first level of flue gas heat exchanger 31 and the certain level or the plurality of levels of low-pressure heaters 7 are in series or parallel connection or in series or parallel connection in the condensed water flow. The flue gas passes through the first-stage flue gas heat exchanger 31, enters the dust collector 300, and enters the second-stage flue gas heat exchanger 32 after the pressure of the flue gas is increased by the draught fan 5 and the desulfurization booster fan 6. In this scheme, booster fan 6 can omit, adopts the higher draught fan 5 of lift to accomplish the function that promotes flue gas pressure. The second-stage flue gas heat exchanger 32 uses flue gas-condensed water as a heat exchange medium, and the flue gas side releases heat and the condensed water side absorbs heat. The flue gas comes from the flue gas at the outlet of the booster fan 6 or the induced draft fan 5. The condensed water comes from a turbine condensed water system, namely, from the outlet of a certain level of low-pressure heater 7 or the outlets of a plurality of levels of low-pressure heaters 7 and is gathered, the condensed water returns to the inlet or the outlet of the certain level of low-pressure heater 7 after absorbing heat through the second level of flue gas heat exchanger 32, namely, the second level of flue gas heat exchanger 32 and the certain level or the plurality of levels of low-pressure heaters 7 are in series or parallel connection or in series or parallel connection in the condensed water flow.
In the scheme, the two stages of flue gas heat exchangers are connected in series in a flue gas flow and connected in parallel in a condensed water flow.
The resistance of the condensate system of the scheme can be overcome by a condensate pump 14 in the turbine condensate system, and a condensate booster pump 8 can be additionally arranged and overcome by the condensate booster pump 8, and the schemes also belong to the protection scope of the invention.
The condensate in this scheme plays and reduces the flue gas temperature, improves the effect of condensate temperature simultaneously. Other types of water sources, such as condensed water of a turbine system of an adjacent machine, heat supply network water, domestic water required by power plants and other units, and the like can also be used as a water source at the water side of the flue gas heat exchanger, and the schemes also belong to the protection scope of the invention.
The selection of which stage of low-pressure heater outlet or which stages of low-pressure heater outlets the condensed water flows from and the heat exchange area required by the flue gas heat exchanger depend on the following factors: (1) the condensate temperature of these take-offs; (2) the flue gas temperature at the inlet and the outlet of the flue gas heat exchanger; (3) the purchase cost of the flue gas heat exchanger; (4) the steam turbine generator unit saves energy consumption or electric power which can be generated more because the steam extraction of the steam turbine is reduced due to the rising of the temperature of the condensed water; (5) the increased power consumption of the fan and condensate pump 14 due to the increased resistance on the flue gas side and the condensate side of the flue gas heat exchanger system; (6) the profit brought by the water consumption saved by the desulfurization system; (7) the dust remover reduces the benefit brought by the emission of smoke and dust; (8) the desulfurization tower improves the benefits brought by desulfurization efficiency; (9) other changes of the equipment configuration and the system configuration of the thermodynamic system and the smoke system of the power plant are caused by the arrangement of the scheme.
Example 2 (corresponding to FIGS. 5 and 6)
The flue gas generated by the combustion of the boiler 100 passes through the air preheater 2, and the temperature is generally between 110 ℃ and 170 ℃ according to the type of the boiler and the type of the fire coal. The temperature of the flue gas is reduced to about 10 ℃ above the acid dew point temperature of the flue gas after passing through the first-stage flue gas heat exchanger 31. The first stage flue gas heat exchanger 31 is an indirect-type flue gas-condensed water heat exchanger with an intermediate carrier, and the intermediate carrier absorbs heat from the flue gas side and heats condensed water. The flue gas is derived from boiler flue gas at the outlet of the air preheater. The condensed water is from a turbine condensed water system, namely from the outlet of a certain level of low-pressure heater 7 or the outlets of a plurality of levels of low-pressure heaters 7 and gathered, the condensed water returns to the inlet or the outlet of the certain level of low-pressure heater 7 after absorbing heat through the first level of flue gas heat exchanger 31, namely the first level of flue gas heat exchanger 31 and the certain level or the plurality of levels of low-pressure heaters 7 are in series or parallel connection or in series or parallel connection in the condensed water flow. The flue gas passes through the first-stage flue gas heat exchanger 31, enters the dust collector 300, and enters the second-stage flue gas heat exchanger 32 after the pressure of the flue gas is increased by the draught fan 5 and the desulfurization booster fan 6. In this scheme, booster fan 6 can omit, adopts the higher draught fan 5 of lift to accomplish the function that promotes flue gas pressure. The second stage flue gas heat exchanger is an indirect type flue gas-condensed water heat exchanger with an intermediate carrier, and the intermediate carrier absorbs heat on the side of the flue gas and heats condensed water. The flue gas comes from the flue gas at the outlet of a booster fan or a draught fan. The condensed water comes from a turbine condensed water system, namely, from the outlet of a certain level of low-pressure heater 7 or the outlets of a plurality of levels of low-pressure heaters 7 and is gathered, the condensed water returns to the inlet or the outlet of the certain level of low-pressure heater 7 after absorbing heat through the second level of flue gas heat exchanger 32, namely, the second level of flue gas heat exchanger 32 and the certain level or the plurality of levels of low-pressure heaters 7 are in series or parallel connection or in series or parallel connection in the condensed water flow.
In the scheme, the two stages of flue gas heat exchangers are connected in series in a flue gas flow and connected in parallel in a condensed water flow.
The resistance of the condensate system of the scheme can be overcome by a condensate pump 14 in the turbine condensate system, and a condensate booster pump 8 can be additionally arranged and overcome by the condensate booster pump 8, and the schemes also belong to the protection scope of the invention.
The intermediate carrier in the scheme is in a liquid state, can be water, and can also be other low-boiling point liquids, such as glycol and the like, and the intermediate carrier is maintained to flow between the flue gas side heat exchanger and the water side heat exchanger through a circulating pump. If low boiling point liquid is adopted, a gas-liquid condensation separation device can be arranged on the circulation loop, and the circulation pump is arranged at the downstream of the device. These solutions also belong to the scope of protection of the present invention.
The condensate in this scheme plays and reduces the flue gas temperature, improves the effect of condensate temperature simultaneously. Other types of water sources, such as condensed water of a turbine system of an adjacent machine, heat supply network water, domestic water required by power plants and other units, and the like can also be used as a water source at the water side of the flue gas heat exchanger, and the schemes also belong to the protection scope of the invention.
The selection of which stage of low-pressure heater outlet or which stages of low-pressure heater outlets the condensed water flows from and the heat exchange area required by the flue gas heat exchanger depend on the following factors: (1) the condensate temperature of these take-offs; (2) the flue gas temperature at the inlet and the outlet of the flue gas heat exchanger; (3) the purchase cost of the flue gas heat exchanger; (4) the steam turbine generator unit saves energy consumption or electric power which can be generated more because the steam extraction of the steam turbine is reduced due to the rising of the temperature of the condensed water; (5) the power consumption of a fan and a condensate pump is increased due to the increased resistance of the flue gas side and the condensate side of the flue gas heat exchanger system; (6) the profit brought by the water consumption saved by the desulfurization system; (7) the dust remover reduces the benefit brought by the emission of smoke and dust; (8) the desulfurization tower improves the benefits brought by desulfurization efficiency; (9) other changes of the equipment configuration and the system configuration of the thermodynamic system and the smoke system of the power plant are caused by the arrangement of the scheme.
Example 3 (corresponding to FIG. 7)
The flue gas generated by the combustion of the boiler 100 passes through the air preheater 2, and the temperature is generally between 110 ℃ and 170 ℃ according to the type of the boiler and the type of the fire coal. The temperature of the flue gas is reduced to about 10 ℃ above the acid dew point temperature of the flue gas after the flue gas passes through the first-stage flue gas heat exchanger. The first stage flue gas heat exchanger 31 is formed by taking flue gas-condensed water as a heat exchange medium, and the flue gas side releases heat and the condensed water side absorbs heat. The flue gas is derived from boiler flue gas at the outlet of the air preheater. The condensed water comes from a turbine condensed water system, namely, from the outlet of a certain stage of low-pressure heater 7 or the outlets of a plurality of stages of low-pressure heaters 7 and is collected, and the condensed water absorbs heat through the first stage flue gas heat exchanger 31 and then enters the inlet of the second stage flue gas heat exchanger 32. The flue gas passes through the first-stage flue gas heat exchanger 31, enters the dust collector 300, and enters the second-stage flue gas heat exchanger 32 after the pressure of the flue gas is increased by the induced draft fan and the desulfurization booster fan. In this scheme, booster fan can omit, adopts the higher draught fan of lift to accomplish the function that promotes flue gas pressure. The second stage flue gas heat exchanger 32 uses flue gas-condensed water as a heat exchange medium, and the flue gas side releases heat and the condensed water side absorbs heat. The flue gas comes from the flue gas at the outlet of a booster fan or a draught fan. The condensed water comes from the condensed water outlet of the first-stage flue gas heat exchanger 31, or is gathered with the condensed water at the outlet of a certain-stage low-pressure heater 7 or the outlets of a plurality of stages of low-pressure heaters 7, and the condensed water returns to the inlet or the outlet of the certain-stage low-pressure heater 7 after absorbing heat through the second-stage flue gas heat exchanger 32. The first stage flue gas heat exchanger 31 and the second stage flue gas heat exchanger 32 are connected in series or in parallel or in series and in parallel with the low pressure heater 7 of a certain stage or a plurality of stages in the condensed water flow.
In the scheme, the two stages of flue gas heat exchangers are connected in series in a flue gas flow path and are also connected in series in a condensed water flow path. For a two-stage flue gas heat exchanger, the flow direction of flue gas and condensed water is concurrent flow.
The resistance of the condensate system of the scheme can be overcome by a condensate pump 14 in the turbine condensate system, and a condensate booster pump 8 can be additionally arranged and overcome by the condensate booster pump 8, and the schemes also belong to the protection scope of the invention.
The condensate in this scheme plays and reduces the flue gas temperature, improves the effect of condensate temperature simultaneously. Other types of water sources, such as condensed water of a turbine system of an adjacent machine, heat supply network water, domestic water required by power plants and other units, and the like can also be used as a water source at the water side of the flue gas heat exchanger, and the schemes also belong to the protection scope of the invention.
The selection of which stage of low-pressure heater outlet or which stages of low-pressure heater outlets the condensed water flows from and the heat exchange area required by the flue gas heat exchanger depend on the following factors: (1) the condensate temperature of these take-offs; (2) the flue gas temperature at the inlet and the outlet of the flue gas heat exchanger; (3) the purchase cost of the flue gas heat exchanger; (4) the steam turbine generator unit saves energy consumption or electric power which can be generated more because the steam extraction of the steam turbine is reduced due to the rising of the temperature of the condensed water; (5) the power consumption of a fan and a condensate pump is increased due to the increased resistance of the flue gas side and the condensate side of the flue gas heat exchanger system; (6) the profit brought by the water consumption saved by the desulfurization system; (7) the dust remover reduces the benefit brought by the emission of smoke and dust; (8) the desulfurization tower improves the benefits brought by desulfurization efficiency; (9) other changes of the equipment configuration and the system configuration of the thermodynamic system and the smoke system of the power plant are caused by the arrangement of the scheme.
Example 4 (corresponding to FIG. 8)
The flue gas generated by the combustion of the boiler 100 passes through the air preheater 2, and the temperature is generally between 110 ℃ and 170 ℃ according to the type of the boiler and the type of the fire coal. The temperature of the flue gas is reduced to about 10 ℃ above the acid dew point temperature of the flue gas after passing through the first-stage flue gas heat exchanger 31. The first stage flue gas heat exchanger 31 is an indirect-type flue gas-condensed water heat exchanger with an intermediate carrier, and the intermediate carrier absorbs heat from the flue gas side and heats condensed water. The flue gas is derived from boiler flue gas at the outlet of the air preheater. The condensed water comes from a turbine condensed water system, namely, from the outlet of a certain stage of low-pressure heater or the outlets of a plurality of stages of low-pressure heaters 7 and is collected, and the condensed water returns to the inlet of the second stage of flue gas heat exchanger 32 after absorbing heat through the first stage of flue gas heat exchanger 31. The flue gas passes through the first-stage flue gas heat exchanger 31, enters the dust collector 300, and enters the second-stage flue gas heat exchanger 32 after the pressure of the flue gas is increased by the induced draft fan and the desulfurization booster fan. In this scheme, booster fan can omit, adopts the higher draught fan of lift to accomplish the function that promotes flue gas pressure. The second stage flue gas heat exchanger 32 is an indirect-type flue gas-condensed water heat exchanger with an intermediate carrier, and the intermediate carrier absorbs heat from the flue gas side and heats condensed water. The flue gas comes from the flue gas at the outlet of a booster fan or a draught fan. The condensed water comes from the outlet of the first-stage flue gas heat exchanger 31, or is gathered with the condensed water at the outlet of a certain-stage low-pressure heater 7 or the outlets of a plurality of stages of low-pressure heaters 7, and the condensed water returns to the inlet or the outlet of the certain-stage low-pressure heater 7 after absorbing heat through the second-stage flue gas heat exchanger 32. The first stage flue gas heat exchanger 31 and the second stage flue gas heat exchanger 32 are connected in series or in parallel or in series and in parallel with the low pressure heater 7 of a certain stage or a plurality of stages in the condensed water flow.
In the scheme, the two stages of flue gas heat exchangers are connected in series in a flue gas flow path and are also connected in series in a condensed water flow path. For a two-stage flue gas heat exchanger, the flow direction of flue gas and condensed water is concurrent flow.
The resistance of the condensate system of the scheme can be overcome by a condensate pump 14 in the turbine condensate system, and a condensate booster pump 8 can be additionally arranged and overcome by the condensate booster pump 8, and the schemes also belong to the protection scope of the invention.
The intermediate carrier in the scheme is in a liquid state, can be water, and can also be other low-boiling point liquids, such as glycol and the like, and the intermediate carrier is maintained to flow between the flue gas side heat exchanger and the water side heat exchanger through a circulating pump. If low boiling point liquid is adopted, a gas-liquid condensation separation device can be arranged on the circulation loop, and the circulation pump is arranged at the downstream of the device. These solutions also belong to the scope of protection of the present invention.
The condensate in this scheme plays and reduces the flue gas temperature, improves the effect of condensate temperature simultaneously. Other types of water sources, such as condensed water of a turbine system of an adjacent machine, heat supply network water, domestic water required by power plants and other units, and the like can also be used as a water source at the water side of the flue gas heat exchanger, and the schemes also belong to the protection scope of the invention.
The selection of which stage of low-pressure heater outlet or which stages of low-pressure heater outlets the condensed water flows from and the heat exchange area required by the flue gas heat exchanger depend on the following factors: (1) the condensate temperature of these take-offs; (2) the flue gas temperature at the inlet and the outlet of the flue gas heat exchanger; (3) the purchase cost of the flue gas heat exchanger; (4) the steam turbine generator unit saves energy consumption or electric power which can be generated more because the steam extraction of the steam turbine is reduced due to the rising of the temperature of the condensed water; (5) the power consumption of a fan and a condensate pump is increased due to the increased resistance of the flue gas side and the condensate side of the flue gas heat exchanger system; (6) the profit brought by the water consumption saved by the desulfurization system; (7) the dust remover reduces the benefit brought by the emission of smoke and dust; (8) the desulfurization tower improves the benefits brought by desulfurization efficiency; (9) other changes of the equipment configuration and the system configuration of the thermodynamic system and the smoke system of the power plant are caused by the arrangement of the scheme.
Example 5 (corresponding to FIG. 9)
The flue gas generated by the combustion of the boiler 100 passes through the air preheater 2, and the temperature is generally between 110 ℃ and 170 ℃ according to the type of the boiler and the type of the fire coal. The temperature of the flue gas is reduced to about 10 ℃ above the acid dew point temperature of the flue gas after passing through the first-stage flue gas heat exchanger 31. The first stage flue gas heat exchanger 31 is formed by taking flue gas-condensed water as a heat exchange medium, and the flue gas side releases heat and the condensed water side absorbs heat. The flue gas is derived from boiler flue gas at the outlet of the air preheater. The condensed water comes from the outlet of the second-stage flue gas heat exchanger 32, or is gathered with the condensed water at the outlet of a certain-stage low-pressure heater 7 or the outlets of a plurality of stages of low-pressure heaters 7, and the condensed water returns to the inlet or the outlet of the certain-stage low-pressure heater 7 after absorbing heat through the first-stage flue gas heat exchanger 31. The flue gas passes through the first-stage flue gas heat exchanger 31, enters the dust collector 300, and enters the second-stage flue gas heat exchanger 32 after the pressure of the flue gas is increased by the induced draft fan and the desulfurization booster fan. In this scheme, booster fan can omit, adopts the higher draught fan of lift to accomplish the function that promotes flue gas pressure. The second stage flue gas heat exchanger 32 uses flue gas-condensed water as a heat exchange medium, and the flue gas side releases heat and the condensed water side absorbs heat. The flue gas comes from the flue gas at the outlet of a booster fan or a draught fan. The condensed water comes from a turbine condensed water system, namely, from the outlet of a certain stage of low-pressure heater 7 or the outlets of a plurality of stages of low-pressure heaters 7 and is collected, and the condensed water absorbs heat through the second stage of flue gas heat exchanger 32 and then reaches the inlet of the first stage of flue gas heat exchanger 31. The first stage flue gas heat exchanger 31 and the second stage flue gas heat exchanger 32 are connected in series or in parallel or in series and in parallel with the low pressure heater 7 of a certain stage or a plurality of stages in the condensed water flow.
In the scheme, the two stages of flue gas heat exchangers are connected in series in a flue gas flow path and are also connected in series in a condensed water flow path. For a two-stage flue gas heat exchanger, the flow direction of flue gas and condensed water is countercurrent.
The resistance of the condensate system of the scheme can be overcome by a condensate pump 14 in the turbine condensate system, and a condensate booster pump 8 can be additionally arranged and overcome by the condensate booster pump 8, and the schemes also belong to the protection scope of the invention.
The condensate in this scheme plays and reduces the flue gas temperature, improves the effect of condensate temperature simultaneously. Other types of water sources, such as condensed water of a turbine system of an adjacent machine, heat supply network water, domestic water required by power plants and other units, and the like can also be used as a water source at the water side of the flue gas heat exchanger, and the schemes also belong to the protection scope of the invention.
The selection of which stage of low-pressure heater outlet or which stages of low-pressure heater outlets the condensed water flows from and the heat exchange area required by the flue gas heat exchanger depend on the following factors: (1) the condensate temperature of these take-offs; (2) the flue gas temperature at the inlet and the outlet of the flue gas heat exchanger; (3) the purchase cost of the flue gas heat exchanger; (4) the steam turbine generator unit saves energy consumption or electric power which can be generated more because the steam extraction of the steam turbine is reduced due to the rising of the temperature of the condensed water; (5) the power consumption of a fan and a condensate pump is increased due to the increased resistance of the flue gas side and the condensate side of the flue gas heat exchanger system; (6) the profit brought by the water consumption saved by the desulfurization system; (7) the dust remover reduces the benefit brought by the emission of smoke and dust; (8) the desulfurization tower improves the benefits brought by desulfurization efficiency; (9) other changes of the equipment configuration and the system configuration of the thermodynamic system and the smoke system of the power plant are caused by the arrangement of the scheme.
Example 6 (corresponding to FIG. 10)
The flue gas generated by the combustion of the boiler 100 passes through the air preheater 2, and the temperature is generally between 110 ℃ and 170 ℃ according to the type of the boiler and the type of the fire coal. The temperature of the flue gas is reduced to about 10 ℃ above the acid dew point temperature of the flue gas after passing through the first-stage flue gas heat exchanger 31. The first stage flue gas heat exchanger 31 is an indirect-type flue gas-condensed water heat exchanger with an intermediate carrier, and the intermediate carrier absorbs heat from the flue gas side and heats condensed water. The flue gas is derived from boiler flue gas at the outlet of the air preheater. The condensed water comes from the outlet of the second-stage flue gas heat exchanger 32, or is gathered with the condensed water at the outlet of a certain-stage low-pressure heater or the outlets of a plurality of stages of low-pressure heaters 7, and the condensed water returns to the inlet or the outlet of the certain-stage low-pressure heater 7 after absorbing heat through the first-stage flue gas heat exchanger 31. The flue gas passes through the first-stage flue gas heat exchanger 31, enters the dust collector 300, and enters the second-stage flue gas heat exchanger 32 after the pressure of the flue gas is increased by the induced draft fan and the desulfurization booster fan. In this scheme, booster fan can omit, adopts the higher draught fan of lift to accomplish the function that promotes flue gas pressure. The second stage flue gas heat exchanger 32 is an indirect-type flue gas-condensed water heat exchanger with an intermediate carrier, and the intermediate carrier absorbs heat from the flue gas side and heats condensed water. The flue gas comes from the flue gas at the outlet of a booster fan or a draught fan. The condensed water comes from a turbine condensed water system, namely, from the outlet of a certain stage of low-pressure heater 7 or the outlets of a plurality of stages of low-pressure heaters 7 and is collected, and the condensed water absorbs heat through the second stage of flue gas heat exchanger 32 and then reaches the inlet of the first stage of flue gas heat exchanger 31. The first stage flue gas heat exchanger 31 and the second stage flue gas heat exchanger 32 are connected in series or in parallel or in series and in parallel with the low pressure heater 7 of a certain stage or a plurality of stages in the condensed water flow.
In the scheme, the two stages of flue gas heat exchangers are connected in series in a flue gas flow path and are also connected in series in a condensed water flow path. For a two-stage flue gas heat exchanger, the flow direction of flue gas and condensed water is countercurrent.
The resistance of the condensate system of the scheme can be overcome by a condensate pump 14 in the turbine condensate system, and a condensate booster pump 8 can be additionally arranged and overcome by the condensate booster pump 8, and the schemes also belong to the protection scope of the invention.
The intermediate carrier in the scheme is in a liquid state, can be water, and can also be other low-boiling point liquids, such as glycol and the like, and the intermediate carrier is maintained to flow between the flue gas side heat exchanger and the water side heat exchanger through a circulating pump. If a low boiling point liquid is used, a gas-liquid condensation separation device can be arranged on the circulation loop, and the circulation pump 9 is arranged at the downstream of the device. These solutions also belong to the scope of protection of the present invention.
The condensate in this scheme plays and reduces the flue gas temperature, improves the effect of condensate temperature simultaneously. Other types of water sources, such as condensed water of a turbine system of an adjacent machine, heat supply network water, domestic water required by power plants and other units, and the like can also be used as a water source at the water side of the flue gas heat exchanger, and the schemes also belong to the protection scope of the invention.
The selection of which stage of low-pressure heater outlet or which stages of low-pressure heater outlets the condensed water flows from and the heat exchange area required by the flue gas heat exchanger depend on the following factors: (1) the condensate temperature of these take-offs; (2) the flue gas temperature at the inlet and the outlet of the flue gas heat exchanger; (3) the purchase cost of the flue gas heat exchanger; (4) the steam turbine generator unit saves energy consumption or electric power which can be generated more because the steam extraction of the steam turbine is reduced due to the rising of the temperature of the condensed water; (5) the power consumption of a fan and a condensate pump is increased due to the increased resistance of the flue gas side and the condensate side of the flue gas heat exchanger system; (6) the profit brought by the water consumption saved by the desulfurization system; (7) the dust remover reduces the benefit brought by the emission of smoke and dust; (8) the desulfurization tower improves the benefits brought by desulfurization efficiency; (9) other changes of the equipment configuration and the system configuration of the thermodynamic system and the smoke system of the power plant are caused by the arrangement of the scheme.
Examples of Performance
Taking a certain 1000MW unit as an example, the scheme of the embodiment 5 is adopted to arrange a two-stage flue gas heat exchanger system. The inlet flue gas temperature of the first stage flue gas heat exchanger 31 is 128 ℃, the outlet flue gas temperature is 105 ℃, the inlet flue gas temperature of the second stage flue gas heat exchanger 32 is 110 ℃, and the outlet flue gas temperature is 86 ℃. The temperature of the condensed water at the inlet of the second-stage flue gas heat exchanger 32 is 59.9 ℃, and the temperature of the condensed water at the outlet of the second-stage flue gas heat exchanger 32 passes through the first-stage flue gas heat exchanger 31 and the second-stage flue gas heat exchanger 32 is 82.30 ℃. The two-stage flue gas heat exchanger system can replace 7070KW heat from flue gas, and is used for a steam turbine to increase work. The coal consumption of the standard coal for power generation can be reduced by 1.6g/Kw.h, and each generator set can save about 9000 tons of standard coal every year according to 5500 hours of the annual utilization of the generator sets. Meanwhile, the temperature of the water entering the desulfurization absorption tower is reduced from 128 ℃ to 86 ℃, so that the water consumption of the desulfurization tower can be saved by about 80t/h, which is equivalent to 44 ten thousand tons of water per year. The efficiency of the electrostatic dust collector can be increased from 99.7 percent to 99.86 percent, and the dust concentration of the flue gas at the outlet of the dust collector is reduced by 16.7mg/Nm3Annual emission reduction of dust 136 t.
Discussion of the related Art
The invention is based on the basic principle of thermodynamic cycle of a steam turbine. The condensed water in the turbine condensed water system cools the boiler flue gas and returns to the turbine condensed water system after being heated by the flue gas, and because the rising of the temperature of the condensed water squeezes part of the extracted steam in the low-pressure heater, and the squeezed extracted steam expands in the turbine to do work under the condition that the steam inlet amount of the turbine is not changed, the generated energy of the turbine generator is increased under the condition that the coal consumption of the turbine generator is not changed.
The invention utilizes the heat in the boiler flue gas through the flue gas heat exchanger based on the following technical means:
the temperature of the flue gas is reduced after the flue gas passes through the first-stage flue gas heat exchanger, and the specific resistance of the flue gas is correspondingly reduced. For the electrostatic dust collector, the dust collection efficiency is obviously improved along with the reduction of the specific resistance of the flue gas. Therefore, the first-stage flue gas heat exchanger is arranged at the inlet of the dust remover to reduce the temperature of flue gas, the dust removal efficiency of the dust remover can be improved, and the emission of smoke dust is reduced.
The temperature of the flue gas is reduced after the flue gas passes through the first-stage flue gas heat exchanger, the volume flow of the flue gas is also reduced, and the power consumption of the induced draft fan and the booster fan is reduced. Therefore, the first-stage flue gas heat exchanger is arranged at the inlet of the dust remover to reduce the temperature of flue gas, the power consumption of a draught fan and a booster fan arranged at the downstream of the dust remover can be reduced, and the station service power of a unit can be saved.
The temperature of the flue gas passing through the first-stage flue gas heat exchanger and the second-stage flue gas heat exchanger is reduced, so that the temperature of the flue gas entering the desulfurization absorption tower is reduced. For the wet flue gas desulfurization process, the temperature of the flue gas is required to be reduced to 40-50 ℃ in a desulfurization absorption tower under the spraying action of the slurry of the desulfurizing agent, and the moisture in the slurry is evaporated by the heat release of the flue gas in the process. The higher the flue gas temperature, the greater the evaporation capacity of the moisture in the slurry, and the greater the water consumption of the desulfurization system. Therefore, after the first-stage flue gas heat exchanger and the second-stage flue gas heat exchanger are arranged, the temperature of flue gas entering the desulfurization absorption tower is reduced, the evaporation capacity of water in the desulfurization absorption tower can be reduced, and the water consumption of a desulfurization system is greatly reduced.
The temperature of the flue gas is reduced after the flue gas passes through the first-stage flue gas heat exchanger and the second-stage flue gas heat exchanger, and the volume flow of the flue gas is reduced. After the flue gas enters the desulfurization absorption tower, the flow velocity of the flue gas is reduced, the retention time of the flue gas in a spraying area of the desulfurization tower is increased, namely, the contact time of sulfur dioxide and desulfurization slurry in the flue gas is increased, the desulfurization efficiency of the desulfurization absorption tower can be improved, and the emission of sulfur dioxide is reduced.
The foregoing is merely a preferred embodiment of the invention and is not intended to limit the scope of the invention, which is defined by the claims appended hereto, and any other technical entity or method that is encompassed by the claims as broadly defined herein, or equivalent variations thereof, is contemplated as being encompassed by the claims.
All documents referred to herein are incorporated by reference into this application as if each were individually incorporated by reference. Furthermore, it should be understood that various changes and modifications can be made by those skilled in the art after reading the above disclosure, and equivalents also fall within the scope of the invention as defined by the appended claims.
Claims (10)
1. The utility model provides a be applied to two-stage gas heater system of thermal power factory, is including boiler unit (100), flue gas waste heat utilization unit (200), flue gas dust removal unit (300) and flue gas desulfurization unit (400) that discharge the flue gas, its characterized in that, flue gas waste heat utilization unit (200) include:
-a preheater (2);
-a first stage flue gas heat exchanger (31) arranged at the inlet of the flue gas dust removal unit (300), and a second stage flue gas heat exchanger (32) arranged at the inlet of the flue gas desulfurization unit (400);
wherein,
the first-stage flue gas heat exchanger (31) and the second-stage flue gas heat exchanger (32) are both flue gas-condensed water heat exchangers provided with a heat-releasing flue gas side and a heat-absorbing condensed water side; the water source at the condensed water side is condensed water in a turbine condensed water system; and is
The first-stage flue gas heat exchanger (31) and the second-stage flue gas heat exchanger (32) are connected in one of the following ways:
the flue gas sides of the two are connected in series, and the condensed water sides of the two are connected in parallel; or
The flue gas side and the condensate side of both are connected in series.
2. The flue gas heat exchanger system of claim 1, wherein the water side water source of the first stage flue gas heat exchanger (31) and the second stage flue gas heat exchanger (32) further comprises adjacent turbine system condensate, heat supply network water, heating, ventilation and air conditioning system water, power plants and other domestic water.
3. The flue gas heat exchanger system of claim 1, wherein the condensate is derived from a stage or a collection of stages of low pressure heater outlets of a turbine condensate system.
4. The flue gas heat exchanger system according to claim 1, wherein the first stage flue gas heat exchanger (31) or the second stage flue gas heat exchanger (32) is a surface type heat exchanger.
5. A flue gas heat exchanger system according to claim 1, wherein the first stage flue gas heat exchanger (31) or the second stage flue gas heat exchanger (32) is a heat pipe type heat exchanger.
6. A flue gas heat exchanger system according to claim 1, wherein the first stage flue gas heat exchanger (31) or the second stage flue gas heat exchanger (32) employs an indirect heat exchanger with an intermediate carrier.
7. The flue gas-to-air heat exchanger system of claim 1, wherein each stage of heat exchangers is one heat exchanger, or a plurality of heat exchangers connected in parallel
8. A method of flue gas waste heat recovery using the two-stage flue gas heat exchanger system of claim 1, comprising the steps of:
enabling the flue gas generated by the boiler unit (100) to pass through a preheater (2) in the flue gas waste heat utilization unit (200) to obtain preheated flue gas at the temperature of 110-170 ℃;
the preheated flue gas is subjected to waste heat recovery in a first-stage flue gas heat exchanger (31), so that the temperature of the preheated flue gas is reduced to be 5-10 ℃ above the acid dew point temperature of the flue gas, and first-stage flue gas subjected to waste heat recovery is obtained;
the temperature of the primary flue gas after waste heat recovery is reduced to be 20-25 ℃ above the dew point temperature of water or the required optimal flue gas temperature after passing through a secondary flue gas heat exchanger (32), so that secondary flue gas after waste heat recovery is obtained;
and the flue gas subjected to waste heat recovery in the second stage enters a flue gas desulfurization unit (400).
9. The method according to claim 8, characterized in that an induced draft fan (5) and an optional desulphurization booster fan (6) are arranged downstream of the flue gas dust removal unit (300), so that the flue gas enters the subsequent second-stage flue gas heat exchanger (32) after being subjected to pressure increase by the induced draft fan (5) and the desulphurization booster fan (6).
10. A thermal power plant system comprising the flue gas waste heat utilization system according to claim 1.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010102248592A CN102330968A (en) | 2010-07-12 | 2010-07-12 | Two-stage flue gas heat exchanger system applied to thermal power plant |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010102248592A CN102330968A (en) | 2010-07-12 | 2010-07-12 | Two-stage flue gas heat exchanger system applied to thermal power plant |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN102330968A true CN102330968A (en) | 2012-01-25 |
Family
ID=45482850
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2010102248592A Pending CN102330968A (en) | 2010-07-12 | 2010-07-12 | Two-stage flue gas heat exchanger system applied to thermal power plant |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102330968A (en) |
Cited By (19)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102645112A (en) * | 2012-04-19 | 2012-08-22 | 浙江清科电力科技有限公司 | Waste heat recovery system for improving efficiency of electric dust collector |
| CN102759096A (en) * | 2012-07-24 | 2012-10-31 | 西安交通大学 | Smoke waste heat utilization system |
| CN103939932A (en) * | 2014-04-28 | 2014-07-23 | 中冶华天工程技术有限公司 | Blast furnace gas boiler flue gas waste heat deep recycling system |
| CN104235826A (en) * | 2013-06-13 | 2014-12-24 | 烟台龙源电力技术股份有限公司 | Boiler flue gas waste heat recycling system |
| CN104235827A (en) * | 2013-06-13 | 2014-12-24 | 烟台龙源电力技术股份有限公司 | Boiler smoke waste heat utilization system |
| CN104654340A (en) * | 2015-02-12 | 2015-05-27 | 中国电力工程顾问集团华东电力设计院有限公司 | Tubular GGH (gas-gas heater) system for thermal power plant |
| CN104930539A (en) * | 2015-06-29 | 2015-09-23 | 山东大学 | Coal-fired power plant flue gas heat regenerative system and energy-saving water-saving ultra-clean discharging method |
| CN105457440A (en) * | 2016-01-16 | 2016-04-06 | 杨德俊 | Device for achieving flue gas power generation and removing harmful substance in flue gas simultaneously |
| CN105627341A (en) * | 2016-03-22 | 2016-06-01 | 中国能源建设集团广东省电力设计研究院有限公司 | Dust remover rear flue gas system provided with flue gas heat exchanger |
| CN106322417A (en) * | 2016-08-25 | 2017-01-11 | 关文吉 | Comprehensive heat exchange system for flue gas and blowdown water of power plant boiler as well as heat exchange method |
| CN106382645A (en) * | 2016-08-25 | 2017-02-08 | 关文吉 | Dry flue gas heat exchange system and heat exchange method of boiler of power station |
| CN106439882A (en) * | 2016-08-26 | 2017-02-22 | 舒少辛 | Desulfuration wastewater treatment device utilizing flue gas waste heat |
| CN106765265A (en) * | 2017-01-05 | 2017-05-31 | 东方电气集团东方锅炉股份有限公司 | A kind of low low temperature heat system of ultra-clean discharging fire coal unit open type |
| CN106931424A (en) * | 2017-03-29 | 2017-07-07 | 中国能源建设集团广东省电力设计研究院有限公司 | Thermal power generation system and its heat energy apparatus, flue gas waste heat utilization device |
| CN109718659A (en) * | 2019-02-28 | 2019-05-07 | 华能国际电力股份有限公司玉环电厂 | Plume governing system |
| CN110006265A (en) * | 2019-05-21 | 2019-07-12 | 福建龙净环保股份有限公司 | A kind of ferrosilicon furnace flue gas purification system |
| CN110848725A (en) * | 2019-12-11 | 2020-02-28 | 中国电力工程顾问集团西北电力设计院有限公司 | Multipurpose flue gas waste heat recovery device and recovery method for thermal power plant |
| CN111219720A (en) * | 2020-01-20 | 2020-06-02 | 山东电力工程咨询院有限公司 | Flue gas waste heat utilization system and method for waste incineration power plant |
| CN112176822A (en) * | 2020-09-14 | 2021-01-05 | 重庆质能环保科技有限公司 | Treatment process for preheating waste asphalt mixture by using waste heat of power plant |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101140072A (en) * | 2007-10-25 | 2008-03-12 | 上海外高桥第三发电有限责任公司 | Desulfurize flue gas waste heat recovery system used in fire coal electric generating set |
| CN201251371Y (en) * | 2008-10-17 | 2009-06-03 | 华润电力投资有限公司 | Flue gas pre-cooling system with highly-effective water and energy conservation |
| US20090272114A1 (en) * | 2004-11-29 | 2009-11-05 | Yasuhiro Takeuchi | Heat recovery equipment |
-
2010
- 2010-07-12 CN CN2010102248592A patent/CN102330968A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20090272114A1 (en) * | 2004-11-29 | 2009-11-05 | Yasuhiro Takeuchi | Heat recovery equipment |
| CN101140072A (en) * | 2007-10-25 | 2008-03-12 | 上海外高桥第三发电有限责任公司 | Desulfurize flue gas waste heat recovery system used in fire coal electric generating set |
| CN201251371Y (en) * | 2008-10-17 | 2009-06-03 | 华润电力投资有限公司 | Flue gas pre-cooling system with highly-effective water and energy conservation |
Cited By (23)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102645112B (en) * | 2012-04-19 | 2014-08-27 | 浙江清科电力科技有限公司 | Waste heat recovery system for improving efficiency of electric dust collector |
| CN102645112A (en) * | 2012-04-19 | 2012-08-22 | 浙江清科电力科技有限公司 | Waste heat recovery system for improving efficiency of electric dust collector |
| CN102759096A (en) * | 2012-07-24 | 2012-10-31 | 西安交通大学 | Smoke waste heat utilization system |
| CN102759096B (en) * | 2012-07-24 | 2015-01-07 | 西安交通大学 | Smoke waste heat utilization system |
| CN104235826A (en) * | 2013-06-13 | 2014-12-24 | 烟台龙源电力技术股份有限公司 | Boiler flue gas waste heat recycling system |
| CN104235827A (en) * | 2013-06-13 | 2014-12-24 | 烟台龙源电力技术股份有限公司 | Boiler smoke waste heat utilization system |
| CN103939932A (en) * | 2014-04-28 | 2014-07-23 | 中冶华天工程技术有限公司 | Blast furnace gas boiler flue gas waste heat deep recycling system |
| CN104654340A (en) * | 2015-02-12 | 2015-05-27 | 中国电力工程顾问集团华东电力设计院有限公司 | Tubular GGH (gas-gas heater) system for thermal power plant |
| CN104930539A (en) * | 2015-06-29 | 2015-09-23 | 山东大学 | Coal-fired power plant flue gas heat regenerative system and energy-saving water-saving ultra-clean discharging method |
| CN105457440B (en) * | 2016-01-16 | 2018-06-29 | 湘南学院 | The device of flue gas harmful substance is removed in a kind of flue gas power generation simultaneously |
| CN105457440A (en) * | 2016-01-16 | 2016-04-06 | 杨德俊 | Device for achieving flue gas power generation and removing harmful substance in flue gas simultaneously |
| CN105627341A (en) * | 2016-03-22 | 2016-06-01 | 中国能源建设集团广东省电力设计研究院有限公司 | Dust remover rear flue gas system provided with flue gas heat exchanger |
| CN105627341B (en) * | 2016-03-22 | 2017-10-13 | 中国能源建设集团广东省电力设计研究院有限公司 | Flue gas system after deduster with flue gas heat-exchange unit |
| CN106382645A (en) * | 2016-08-25 | 2017-02-08 | 关文吉 | Dry flue gas heat exchange system and heat exchange method of boiler of power station |
| CN106322417A (en) * | 2016-08-25 | 2017-01-11 | 关文吉 | Comprehensive heat exchange system for flue gas and blowdown water of power plant boiler as well as heat exchange method |
| CN106439882A (en) * | 2016-08-26 | 2017-02-22 | 舒少辛 | Desulfuration wastewater treatment device utilizing flue gas waste heat |
| CN106765265A (en) * | 2017-01-05 | 2017-05-31 | 东方电气集团东方锅炉股份有限公司 | A kind of low low temperature heat system of ultra-clean discharging fire coal unit open type |
| CN106931424A (en) * | 2017-03-29 | 2017-07-07 | 中国能源建设集团广东省电力设计研究院有限公司 | Thermal power generation system and its heat energy apparatus, flue gas waste heat utilization device |
| CN109718659A (en) * | 2019-02-28 | 2019-05-07 | 华能国际电力股份有限公司玉环电厂 | Plume governing system |
| CN110006265A (en) * | 2019-05-21 | 2019-07-12 | 福建龙净环保股份有限公司 | A kind of ferrosilicon furnace flue gas purification system |
| CN110848725A (en) * | 2019-12-11 | 2020-02-28 | 中国电力工程顾问集团西北电力设计院有限公司 | Multipurpose flue gas waste heat recovery device and recovery method for thermal power plant |
| CN111219720A (en) * | 2020-01-20 | 2020-06-02 | 山东电力工程咨询院有限公司 | Flue gas waste heat utilization system and method for waste incineration power plant |
| CN112176822A (en) * | 2020-09-14 | 2021-01-05 | 重庆质能环保科技有限公司 | Treatment process for preheating waste asphalt mixture by using waste heat of power plant |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102330968A (en) | Two-stage flue gas heat exchanger system applied to thermal power plant | |
| CN201715542U (en) | Two-stage flue gas-air heat exchanger system applied to fuel electric plant | |
| CN102313291A (en) | Two-stage smoke-gas-air heat-exchanger system applied to thermal power plant | |
| CN102759096B (en) | Smoke waste heat utilization system | |
| CN102454980B (en) | Method for recycling flue gas waste heat of thermal power plant boiler | |
| CN201795471U (en) | Flue gas afterheat utilization system | |
| CN202177093U (en) | Multi-level efficient displacement type fume waste-heat utilization system | |
| CN109668165B (en) | Hot secondary air and flue gas waste heat utilization system and thermal generator set | |
| CN102734787B (en) | Concurrent recycling system for boiler smoke afterheat | |
| CN202647717U (en) | Thermal power plant waste heat utilization system and thermal power generating unit | |
| CN103574630B (en) | Improve the method for temperature of smoke discharged by chimney of thermal power and flue gas heating system and fired power generating unit | |
| CN104266171A (en) | Flue gas waste heat utilization system of thermal power plant | |
| CN103574587B (en) | Waste heat utilizing system of thermal power plant and thermal power unit | |
| CN105889897B (en) | A kind of thermal power plant residual heat integrative recycling system and method | |
| CN201892201U (en) | Two-level smoke heat exchanger system applied to thermal power plant | |
| CN102678206B (en) | Thermodynamic system for combined heat recovery of power plant | |
| CN202673378U (en) | Waste steam energy utilization system for driving steam turbine in thermal power plant and thermal power generating unit | |
| CN103032867A (en) | Multilevel efficient replaceable type smoke waste heat using system | |
| CN202675925U (en) | Drive turbine steam exhaust cooling system and thermal power generating unit of thermal power plant | |
| CN110986031B (en) | System for avoiding water vapor condensation in gas boiler flue gas recirculation pipeline | |
| CN202791972U (en) | Boiler tail flue gas waste heat utilization system | |
| CN105757645A (en) | Efficient low-grade residual heat resource utilization system for coal-fired power plant | |
| CN103575124A (en) | Steam exhaust cooling system of driving steam turbine of thermal power plant and thermal power unit | |
| CN202733927U (en) | Smoke heating system and thermal power generating unit for increasing exhaust gas temperature of thermal power station chimney | |
| CN211011316U (en) | Steam turbine boiler waste heat utilization system for coal-fired power plant |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C12 | Rejection of a patent application after its publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20120125 |