CN106996551B - Stepped multi-step bubbling bed heat exchange device - Google Patents
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- CN106996551B CN106996551B CN201710353722.9A CN201710353722A CN106996551B CN 106996551 B CN106996551 B CN 106996551B CN 201710353722 A CN201710353722 A CN 201710353722A CN 106996551 B CN106996551 B CN 106996551B
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
- F22B1/00—Methods of steam generation characterised by form of heating method
- F22B1/02—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers
- F22B1/18—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers the heat carrier being a hot gas, e.g. waste gas such as exhaust gas of internal-combustion engines
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
- F22B31/00—Modifications of boiler construction, or of tube systems, dependent on installation of combustion apparatus; Arrangements of dispositions of combustion apparatus
- F22B31/08—Installation of heat-exchange apparatus or of means in boilers for heating air supplied for combustion
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
- F22B37/00—Component parts or details of steam boilers
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22D—PREHEATING, OR ACCUMULATING PREHEATED, FEED-WATER FOR STEAM GENERATION; FEED-WATER SUPPLY FOR STEAM GENERATION; CONTROLLING WATER LEVEL FOR STEAM GENERATION; AUXILIARY DEVICES FOR PROMOTING WATER CIRCULATION WITHIN STEAM BOILERS
- F22D1/00—Feed-water heaters, i.e. economisers or like preheaters
- F22D1/50—Feed-water heaters, i.e. economisers or like preheaters incorporating thermal de-aeration of feed-water
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Abstract
The utility model discloses a heat exchange device of a stepped multi-step bubbling bed, which comprises: the boiler comprises a material hopper, a superheater, an evaporator, an economizer, a preheater and 4 boilers which are sequentially arranged from high to low: the utility model greatly improves the gradient degree of the waste heat transfer process on the premise of not increasing the power consumption, greatly reduces the irreversible loss of cold and heat sources in the heat transfer process, and can improve the utilization rate of the waste heat by 20% -30%. The probability of blocking and wearing the blast cap is greatly reduced, and the accident rate of the blast cap is reduced by 80% -90%. The temperature of particles leaving the cooling device is reduced to about 100 ℃, and the waste heat recovery rate of the device is improved by 10% -20%.
Description
Technical Field
The utility model belongs to the technical field of heat exchange equipment, and particularly relates to a stepped multi-step bubbling bed heat exchange device.
Background
In recent years, some high-temperature and medium-temperature particulate waste heat recycling systems in the industrial field generally adopt a double-layer fluidized bed cooling method, but the existing double-layer fluidized bed cooling method has the problems that the waste heat recycling effect is unsatisfactory and the recycling index is far lower than the international level in practical application. The existing double-layer fluidized bed cooling method has the following main problems: the temperature of the double-layer fluidized bed can only be set to be two constant temperatures, and the temperature difference between the cold heating surface and the inlet and outlet of the heat source in the heat transfer process of each heating surface of the waste heat boiler is set to be larger, so that the irreversible loss in the heat transfer process is increased, and the waste heat utilization efficiency is greatly reduced; the temperature of the low-temperature bed of the double-layer fluidized bed is limited by the temperature of a working medium outlet, namely, the double-layer fluidized bed cooling device cannot lower the temperature of solid particles to be very low, and the waste heat recovery is incomplete, so that the waste heat recovery rate is low; in the double-layer fluidized bed cooling device, two fluidized beds are connected in series, and a low-temperature bed fluidization medium brings a large amount of particles into a blast cap of a high-temperature bed, so that the blast cap of the high-temperature bed is easy to block and abrade.
Disclosure of Invention
Aiming at the defects of the prior art, the utility model aims to provide the stepped multi-step bubbling bed heat exchange device with high waste heat recovery rate and good safety of a high-temperature bed hood.
For this purpose, the technical scheme of the utility model is as follows:
a stepped multi-step bubble-bed heat exchange device comprising: the position is from high to low first through fourth boilers and material hopper, superheater, evaporimeter, economizer and preheater that arrange in proper order, first through fourth boilers all include: the device comprises a sealed cylinder body and a bubbling bed air bin fixedly arranged at the lower end of the cylinder body, wherein an air inlet is formed at the lower end of the bubbling bed air bin, and an air outlet is formed at the upper end of the cylinder body; a plurality of hoods are arranged between the bubbling bed wind bin and the cylinder at intervals, so that gas entering the bubbling bed wind bin from the air inlet is accelerated after passing through the hoods, the gas wind direction is converted into from bottom to top, and the periphery of a filter screen is in sealing connection with the inner wall of the cylinder and is used for filtering solid particles in the gas flowing to the air outlet;
the superheater, the evaporator, the economizer and the preheater are respectively and sequentially arranged in the first boiler, the second boiler, the third boiler and the fourth boiler, the outlet of the preheater is communicated with the inlet of the economizer through a first pipeline, and the first pipeline is provided with a deaerator and a water supply pump so that water passing through the preheater forms saturated water through the economizer; the outlet of the coal economizer is communicated with a water inlet pipe of a steam drum, the descending pipe of the steam drum is communicated with the inlet of the evaporator, the outlet of the evaporator is communicated with the ascending pipe of the steam drum, and the steam outlet of the steam drum is communicated with the inlet of the superheater so that saturated steam discharged from the steam outlet enters the superheater to form superheated steam; the exhaust port of the superheater is communicated with the steam inlet of the steam turbine, the steam outlet of the steam turbine is communicated with the steam inlet of the condenser, the condensed water outlet of the condenser is communicated with the inlet of the preheater through a pipeline, and a condensed water pump is arranged on the pipeline between the condensed water outlet and the inlet of the preheater;
a first bubbling bed fluidization fan is arranged below the air inlet of the second boiler, the air outlet of the second boiler is communicated with the air inlet of the first boiler through a second pipeline, a first dust remover is arranged on the second pipeline, the air outlet of the first boiler is communicated with the second waste heat boiler through a third pipeline, and a second dust remover is arranged on the third pipeline; a second bubbling bed fluidization fan is arranged below the air inlet of the fourth boiler, the air outlet of the fourth boiler is communicated with the air inlet of the third boiler through a fourth pipeline, and a third dust remover is arranged on the fourth pipeline; the air outlet of the third boiler is communicated with the first waste heat boiler through a fifth pipeline, and a fourth dust remover is arranged on the fifth pipeline;
the material hopper is communicated with the first boiler; a cold slag port is formed below the cylinder of the fourth boiler, and the Leng Zhakou is led out of the fourth boiler through a cold slag pipeline;
and overflow pipes are communicated among the cylinders of the first boiler, the second boiler, the third boiler and the fourth boiler, one end of each overflow pipe is communicated with the upper part of the cylinder of the higher boiler in the adjacent boiler, the other end of each overflow pipe is communicated with the lower part of the cylinder of the lower boiler in the adjacent boiler, and both ends of each overflow pipe are positioned below the filter screen in the corresponding boiler.
In the above technical solution, the steam turbine is connected with the generator.
In the above technical solution, the condenser is connected to a cooling tower so that condensation heat is discharged to the atmosphere through the cooling tower.
In the above technical solution, the pressure P of the first waste heat boiler 1 P is more than or equal to 3.8MPa 1 ＜5.3MPa。
In the above technical solution, the pressure P of the second waste heat boiler 2 P is more than or equal to 9.8MPa 2 ＜13.7MPa。
In the above technical solution, the dust outlet of the first dust collector is communicated with an overflow pipe between the second boiler and the third boiler.
In the above technical solution, the dust outlet of the second dust collector is communicated with an overflow pipe between the second boiler and the first boiler.
In the above technical scheme, the dust outlets of the third dust remover and the fourth dust remover are communicated with the overflow pipe between the third boiler and the fourth boiler.
In the above technical solution, the outlet ports of the superheater, the evaporator, the economizer and the preheater are all located above the inlet ports of the corresponding superheater, evaporator, economizer and preheater.
Compared with the prior art, the utility model comprises the following steps:
1) The gradient degree of the waste heat transfer process is greatly improved on the premise of not increasing the power consumption, the irreversible loss of cold and heat sources in the heat transfer process is greatly reduced, and the waste heat utilization rate can be improved by 20% -30%.
2) The probability of blocking and wearing of the blast cap of the high-temperature bed is greatly reduced, and the accident rate of the blast cap is reduced by 80-90%.
3) The temperature of particles leaving the cooling device is reduced to about 100 ℃, and the waste heat recovery rate of the device is improved by 10% -20%.
Drawings
FIG. 1 is a schematic diagram of a heat exchanger of a stepped multi-step bubble-bed.
Wherein, 1: bubbling bed wind bin, 2: hood, 3: material hopper, 4: superheater, 5: overflow pipe, 6: second dust remover, 7: first dust remover, 8: steam drum, 9: condenser, 10: turbine, 11: generator, 12: cooling tower, 13: fourth dust remover, 14: third dust remover, 15: condensate pump, 16: deaerator, 17: preheater, 18: slag cooling pipeline, 19: a second bubbling bed fluidization fan, 20: feed pump, 21: economizer, 22: a first bubbling bed fluidization fan, 23: evaporator, 24: first pipeline, 25: second line, 26: third line, 27: fourth line, 28: fifth line, 29: first exhaust-heat boiler, 30: and a second waste heat boiler.
Detailed Description
In the specific embodiment of the utility model, the recovered high-temperature particles are about 900 ℃, four boilers with sequentially reduced heights and bed temperatures (temperatures) are arranged in the stepped multi-step bubbling bed heat exchange device, a superheater, an evaporator, an economizer and a preheater are respectively embedded in the four boilers according to the sequentially reduced heights and the bed temperatures, the four bubbling bed fluidization mediums are air, wherein the two higher-temperature first boilers and the second boilers (the bubbling bed of the evaporator and the bubbling bed of the superheater) are connected in series, the two lower-temperature third boilers and the fourth boilers (the bubbling bed of the economizer and the bubbling bed of the condensed water) are connected in series, and the high-temperature bubbling mediums and the low-temperature bubbling mediums are mutually independent.
The discharge opening can be used in the present utility model for steam discharge, water discharge or steam-water mixture. The inlet port may be for inlet water, inlet steam or inlet steam water mixture.
The technical scheme of the utility model is further described below with reference to the attached drawings and specific embodiments.
As shown in fig. 1, includes: 4 boilers (bubbling bed boilers) arranged in order from top to bottom: the first, second, third and fourth boilers and the material hopper 3, superheater 4, evaporator 23, economizer 21, preheater 17, the first to fourth boilers each include: the bubbling bed air bin 1 (namely an air bin) is fixedly arranged at the lower end of the sealed cylinder, an air inlet is formed at the lower end of the bubbling bed air bin 1, and an air outlet is formed at the upper end of the cylinder; a plurality of hoods 2 are arranged between the bubbling bed wind bin 1 and the cylinder at intervals, so that gas entering the bubbling bed wind bin 1 from the air inlet is accelerated after passing through the hoods 2, the direction of the gas wind is changed into from bottom to top, and the periphery of a filter screen is in sealing connection with the inner wall of the cylinder and is used for filtering most of solid particles in the gas flowing to the air outlet.
The superheater 4, the evaporator 23, the economizer 21 and the preheater 17 are respectively and sequentially installed in the first boiler, the second boiler, the third boiler and the fourth boiler, an outlet of the preheater 17 for discharging water is communicated with an inlet of the economizer 21 for feeding water through a first pipeline 24, and a deaerator 16 and a feed pump 20 are installed on the first pipeline 24 so that water passing through the preheater 17 passes through the economizer 21 to form saturated water; the outlet of the economizer 21 for discharging water is communicated with a water inlet pipe of a steam drum 8, the descending pipe of the steam drum 8 is communicated with an inlet of an evaporator 23, the outlet of the evaporator 23 for discharging steam is communicated with an ascending pipe of the steam drum 8, and the steam outlet of the steam drum 8 is communicated with an inlet of the superheater 4 for entering steam, so that saturated steam discharged from the steam outlet enters the superheater 4 to form superheated steam; the discharge port of the superheater 4 communicates with the steam inlet of the turbine 10, and the turbine 10 is connected to the generator 11. The steam outlet of the steam turbine 10 is communicated with the steam inlet of the condenser 9, the condensed water outlet of the condenser 9 is communicated with the inlet of the preheater 17 through a pipeline, and a condensed water pump 15 is arranged on the pipeline between the condensed water outlet and the inlet of the preheater 17; the condenser 9 is connected to a cooling tower 12 so that condensation heat is discharged to the atmosphere through the cooling tower 12. The discharge ports of the superheater 4, the evaporator 23, the economizer 21 and the preheater 17 are located above the inlet ports of the respective superheater 4, evaporator 23, economizer 21 and preheater 17.
A first bubbling bed fluidization fan 22 is arranged below the air inlet of the second boiler, the air outlet of the second boiler is communicated with the air inlet of the first boiler through a second pipeline 25, a first dust remover 7 is arranged on the second pipeline 25, and the dust outlet of the first dust remover 7 is communicated with an overflow pipe 5 between the second boiler and a third boiler.
The air outlet of the first boiler is communicated with a second waste heat boiler 30 through a third pipeline 26, and the pressure P of the second waste heat boiler 30 2 P is more than or equal to 9.8MPa 2 < 13.7MPa. . The third pipeline 26 is provided with a second dust remover 6; the dust outlet of the second dust separator 6 communicates with an overflow pipe 5 between the second boiler and the first boiler.
A second bubbling bed fluidization fan 19 is arranged below the air inlet of the fourth boiler, the air outlet of the fourth boiler is communicated with the air inlet of the third boiler through a fourth pipeline 27, and a third dust remover 14 is arranged on the fourth pipeline 27; the air outlet of the third boiler is connected with the first surplus through a fifth pipeline 28The heat boiler 29 is communicated with the pressure P of the first waste heat boiler 29 1 P is more than or equal to 3.8MPa 1 Less than 5.3MPa. And a fourth dust remover 13 is arranged on the fifth pipeline 28; the dust outlets of the third dust remover 14 and the fourth dust remover 13 are communicated with the overflow pipe 5 between the third boiler and the fourth boiler.
The material hopper 3 is communicated with the first boiler; a cold slag port is formed below the cylinder of the fourth boiler and is communicated with the outside of the fourth boiler through a cold slag pipeline 18;
and an overflow pipe 5 is communicated between the cylinders of the adjacent first boiler, the second boiler, the third boiler and the fourth boiler, one end of the overflow pipe 5 is communicated with the upper part of the cylinder of the higher boiler in the adjacent boiler, the other end of the overflow pipe 5 is communicated with the lower part of the cylinder of the lower boiler in the adjacent boiler, and the communicated parts at the two ends of the overflow pipe 5 are all positioned below the filter screen in the corresponding boiler.
1) Working medium flow of the embodiment of the utility model
The condensate water is pressurized by a condensate pump 15 and then enters a preheater 17 to exchange heat with the lowest temperature material and is heated, then enters a deaerator 16 to deoxidize to form deoxidized water, the deoxidized water is pressurized by a feed pump 20 and enters an economizer 21 to exchange heat with the next low temperature material to heat and raise the temperature to form saturated water, the saturated water enters a steam drum 8, in the steam drum, the saturated water enters an evaporator 23 through a down pipe of the steam drum to exchange heat and vaporize with the next high temperature material to form a steam-water mixture, the steam-water mixture returns to the steam drum 8 to form saturated steam, the saturated steam is led out of the steam drum 8 to enter a superheater 4 to exchange heat with the high temperature material, the temperature is raised to be superheated steam, the superheated steam leaves the superheater 4 to enter a steam turbine 10 to expand and do work, and is generated by a generator 11, the waste steam of the steam turbine enters a condenser 9 to condense, the condensation heat is discharged into the atmosphere by a cooling tower 12, and the condensed water enters the condensate pump 15 to pressurize to enter the next working cycle.
2) The embodiment of the utility model fluidizes the medium flow
Low temperature bubbling bed fluidization medium scheme 1: the cold air is pressurized by a second bubbling bed fluidization fan 19 and enters a bubbling bed air bin 1 of a fourth boiler, then enters a cylinder of the fourth boiler through a hood 2, fluidizes low-temperature materials in the cylinder of the fourth boiler, and enters a third boiler where an economizer 21 is positioned after the fluidization medium (air) leaves the fourth boiler and is dedusted by a third deduster 14, and enters the cylinder of the third boiler through the hood to fluidize the sub-low-temperature materials in the cylinder of the third boiler; after leaving the third boiler, the fluidizing medium is dedusted by the fourth deduster 13 to form clean medium temperature air, which is finally sent to the medium temperature gas waste heat boiler to generate medium pressure steam, namely the first waste heat boiler 29.
High temperature bubbling bed fluidization medium scheme 2: cold air is pressurized by a first bubbling bed fluidization fan 22 and enters a bubbling bed air bin 1 of a second boiler, then enters a cylinder of the second boiler where an evaporator 23 is located by a hood 2 to fluidize secondary high-temperature materials, fluidization medium enters the cylinder of the first boiler after leaving the second boiler and being dedusted by a first deduster 7 to fluidize the highest-temperature materials, after leaving the first boiler, fluidization medium is dedusted by a second deduster 6 to form clean high-temperature air, and finally the high-temperature air is sent to a high-temperature gas waste heat boiler to generate high-pressure steam, namely a second waste heat boiler 30.
3) The embodiment of the utility model relates to a high-temperature particle flow
The high-temperature particles enter a first boiler where a superheater with the highest temperature is located from a material hopper 3, heat exchange is carried out between the high-temperature particles and superheated steam and a fluidization medium (air) in a superheater 4 in the first boiler, then the high-temperature particles enter a second boiler where an evaporator with the next highest temperature is located through an overflow pipe 5, and in the second boiler, heat exchange is carried out between the high-temperature particles and saturated water and the fluidization medium in the evaporator. The high-temperature particles enter a third boiler where the economizer 21 with the next lower temperature is positioned through the overflow pipe 5, heat exchange is carried out between the third boiler and unsaturated water and fluidization medium in the economizer 21, then the high-temperature particles enter a fourth boiler where the preheater 17 with the lowest temperature is positioned through the overflow pipe 5, heat exchange is carried out between the fourth boiler and condensation water and fluidization medium in the preheater 17, and finally the whole stepped multi-step bubbling bed heat exchange device is discharged through the slag cooling pipeline 18.
The technical scheme adopted for solving the defects in the prior art is as follows:
1. in the original double-fluidized bed device, two fluidized bed solid particles and a fluidized medium are connected in series: the solid particles leave the high-temperature bed and directly enter the low-temperature bed through the ash dropping pipe, and the low-temperature bed fluidization medium leaves the low-temperature bed and directly enters the high-temperature bed through the high-temperature bed hood. The double-series structure determines that the more the series stage number is, the larger the fluidization wind resistance is, the more the electricity consumption is, and the more the blast cap is worn, so that only a double-layer fluidized bed is arranged. The utility model changes the connection mode between adjacent fluidized beds, adopts 4 ladder-shaped boilers to realize multi-step bed temperature of solid particles, and connects the solid particles of adjacent two-stage boilers in series: the upper boiler enters the adjacent lower boiler through the middle overflow pipe. However, all the fluidizing gas of the adjacent boilers are not in a serial connection mode, the fluidizing medium of each boiler is independently fed in and fed out of each boiler, the two stages of adjacent boilers are in serial connection, and the fluidizing gas of the other boilers is independent of the flow of the fluidizing gas of the other boilers, when the two stages of adjacent boilers are in serial connection, the fluidizing gas discharged from the low-temperature boiler firstly enters the dust remover to separate gas from solid by utilizing cyclone, and then enters the adjacent higher-temperature boiler, so that the probability of blocking and wearing of the blast caps of the high-temperature boiler is reduced.
2. After the bubbling bed (boiler) fluidization medium is changed into parallel connection in series, 4 bubbling bed heat exchangers with gradually reduced bed temperature can be adopted to better realize the cascade heat exchange of particles and working medium. The structure can realize the heat exchange of the superheater, the evaporator, the economizer and the condensate preheater of working medium in turn by adopting 4 boilers (bubbling beds), so that the gradient degree of the waste heat transfer process is greatly improved on the premise of not increasing the power consumption, the irreversible loss of cold and heat sources in the heat transfer process is greatly reduced, and the utilization rate of the waste heat can be improved by 20% -30%.
3. In the stepped multi-step bed temperature heat exchange device, the boiler positioned at the lowest part can independently heat the condensed water before entering the deaerator by utilizing the low-temperature waste heat of particles, so that the temperature of the particles is reduced to a low temperature which is approximately 100 ℃, and the waste heat recovery rate is greatly improved.
The foregoing has described exemplary embodiments of the utility model, it being understood that any simple variations, modifications, or other equivalent arrangements which would not unduly obscure the utility model may be made by those skilled in the art without departing from the spirit of the utility model.
Claims (9)
1. A stepped multi-step bubble-bed heat exchange device, comprising: first to fourth boilers and material hoppers (3), superheaters (4), evaporators (23), economizers (21) and preheaters (17) arranged in this order from high to low, the first to fourth boilers each comprising: the device comprises a sealed cylinder body and a bubbling bed air bin (1) fixedly arranged at the lower end of the cylinder body, wherein an air inlet is formed at the lower end of the bubbling bed air bin (1), and an air outlet is formed at the upper end of the cylinder body; a plurality of hoods (2) are arranged between the bubbling bed wind bin (1) and the cylinder at intervals, so that gas entering the bubbling bed wind bin (1) from the air inlet is accelerated after passing through the hoods (2) and the gas wind direction is converted into from bottom to top, and the periphery of a filter screen is in sealing connection with the inner wall of the cylinder and is used for filtering solid particles in the gas flowing to the air outlet;
the superheater (4), the evaporator (23), the economizer (21) and the preheater (17) are respectively and sequentially arranged in the first boiler, the second boiler, the third boiler and the fourth boiler, the outlet of the preheater (17) is communicated with the inlet of the economizer (21) through a first pipeline (24), and a deaerator (16) and a water supply pump (20) are arranged on the first pipeline (24) so that water passing through the preheater (17) passes through the economizer (21) to form saturated water; the exhaust port of the economizer (21) is communicated with the water inlet pipe of a steam drum (8), the descending pipe of the steam drum (8) is communicated with the inlet port of the evaporator (23), the exhaust port of the evaporator (23) is communicated with the ascending pipe of the steam drum (8), and the steam outlet of the steam drum (8) is communicated with the inlet port of the superheater (4) so that saturated steam exhausted from the steam outlet enters the superheater (4) to form superheated steam; the exhaust port of the superheater (4) is communicated with the steam inlet of the steam turbine (10), the steam outlet of the steam turbine (10) is communicated with the steam inlet of the condenser (9), the condensed water outlet of the condenser (9) is communicated with the inlet of the preheater (17) through a pipeline, and a condensed water pump (15) is arranged on the pipeline between the condensed water outlet and the inlet of the preheater (17);
a first bubbling bed fluidization fan (22) is arranged below the air inlet of the second boiler, the air outlet of the second boiler is communicated with the air inlet of the first boiler through a second pipeline (25), a first dust remover (7) is arranged on the second pipeline (25), the air outlet of the first boiler is communicated with a second waste heat boiler (30) through a third pipeline (26), and a second dust remover (6) is arranged on the third pipeline (26); a second bubbling bed fluidization fan (19) is arranged below the air inlet of the fourth boiler, the air outlet of the fourth boiler is communicated with the air inlet of the third boiler through a fourth pipeline (27), and a third dust remover (14) is arranged on the fourth pipeline (27); the air outlet of the third boiler is communicated with the first waste heat boiler (29) through a fifth pipeline (28), and a fourth dust remover (13) is arranged on the fifth pipeline (28);
the material hopper (3) is communicated with the first boiler; a cold slag port is formed below the cylinder of the fourth boiler, and the Leng Zhakou is led out of the fourth boiler through a cold slag pipeline (18);
an overflow pipe (5) is communicated between the cylinders of the first boiler, the second boiler, the third boiler and the fourth boiler, one end of the overflow pipe (5) is communicated with the upper part of the cylinder of the boiler with higher position in the adjacent boiler, the other end of the overflow pipe is communicated with the lower part of the cylinder of the boiler with lower position in the adjacent boiler, and both ends of the overflow pipe (5) are positioned below the filter screen in the corresponding boiler;
the first boiler is an evaporator bubbling bed, the second boiler is a superheater bubbling bed, the third boiler is an economizer bubbling bed, and the fourth boiler is a condensate preheater bubbling bed;
the evaporator bubbling bed is connected with the superheater bubbling bed fluidization medium in series, and the economizer bubbling bed is connected with the condensate water preheater bubbling bed fluidization medium in series;
the evaporator bubbling bed, the superheater bubbling bed, the economizer bubbling bed and the condensate preheater bubbling bed are air.
2. The stepped multi-step bubble-bed heat exchange device according to claim 1, wherein the steam turbine (10) is connected to an electric generator (11).
3. The stepped multi-step bubble-bed heat exchange device according to claim 1 or 2, wherein the condenser (9) is connected to a cooling tower (12), through which cooling tower (12) the condensation heat is discharged to the atmosphere.
4. The stepped multi-step bubble-bed heat exchange device according to claim 3, wherein the pressure P1 of the first waste heat boiler (29) is 3.8 mpa.ltoreq.p1 < 5.3MPa.
5. The stepped multi-step bubble-bed heat exchange device of claim 4, wherein the pressure P2 of said second heat recovery boiler (30) is 9.8 MPa-P2 < 13.7MPa.
6. The stepped multi-step bubble-bed heat exchange device according to claim 5, wherein the dust outlet of the first dust separator (7) communicates with an overflow pipe (5) between the second and third boilers.
7. The stepped multi-step bubble-bed heat exchange device according to claim 6, wherein the dust outlet of the second dust separator (6) communicates with an overflow pipe (5) between the second boiler and the first boiler.
8. The stepped multi-step bubble-bed heat exchange device according to claim 7, wherein dust outlets of the third dust remover (14) and the fourth dust remover (13) are both in communication with an overflow pipe (5) between the third boiler and the fourth boiler.
9. The stepped multi-step bubble column heat exchange device of claim 8, wherein the vapor water outlets of the superheater (4), the evaporator (23), the economizer (21) and the preheater (17) are all located above vapor water inlet ports of the respective superheater (4), evaporator (23), economizer (21) and preheater (17).
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| CN104776412B (en) * | 2015-04-14 | 2016-06-08 | 余传林 | A kind of high temperature superfine powder heat recovery boiler |
| CN105154606B (en) * | 2015-10-14 | 2017-05-03 | 华北理工大学 | Blast furnace slag space atomization water quenching and high-temperature water quenching slag waste heat power generating method |
| CN206724124U (en) * | 2017-05-18 | 2017-12-08 | 华北理工大学 | The more step bed temperature bubbling bed heat-exchanger rigs of staged |
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2017
- 2017-05-18 CN CN201710353722.9A patent/CN106996551B/en active Active
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