CN218106766U - Energy recovery system for gasification black water four-stage flash evaporation - Google Patents
Energy recovery system for gasification black water four-stage flash evaporation Download PDFInfo
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- CN218106766U CN218106766U CN202222604311.1U CN202222604311U CN218106766U CN 218106766 U CN218106766 U CN 218106766U CN 202222604311 U CN202222604311 U CN 202222604311U CN 218106766 U CN218106766 U CN 218106766U
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Abstract
The utility model belongs to an energy recovery system for four-stage flash evaporation of gasified black water; the system comprises a gasified black water pipeline and an ash water pipeline, wherein the gasified black water pipeline is connected with a lower tower inlet of an evaporation hot water tower, the ash water pipeline is connected with an upper tower inlet of the evaporation hot water tower, a liquid phase outlet at the bottom of the evaporation hot water tower is connected with an inlet of a first-stage low-pressure flash tank, a liquid phase outlet at the bottom of the first-stage low-pressure flash tank is connected with an inlet of a second-stage low-pressure flash tank, a liquid phase outlet at the bottom of the second-stage low-pressure flash tank is connected with an inlet of a vacuum flash tank, a gas phase outlet of the vacuum flash tank is connected with an inlet of a third gas-liquid separation tank through an ultra-low pressure turbine and a vacuum flash condenser, a liquid phase outlet of the third gas-liquid separation tank is connected with a condensate recovery tank, and a gas phase outlet of the third gas-liquid separation tank is connected with a vacuum pumping system; the energy-saving and energy-saving recycling system has the advantages of simple structure, reasonable design, energy conservation, consumption reduction and energy recycling on the premise of ensuring the normal and stable operation of the whole system.
Description
Technical Field
The utility model belongs to the technical field of coal gasification, in particular to energy recovery system is used in flash distillation of gasification black water level four.
Background
The coal gasification technology comprises two processes of pulverized coal gasification and coal water slurry gasification, wherein the two processes comprise the working procedures and devices of raw coal treatment, synthesis gas production and washing, black ash water treatment and the like; the black water of the gasification furnace and the water scrubber generally needs to be subjected to secondary or tertiary flash evaporation in the black and gray water treatment process, so that the purpose of removing acid gases such as carbon dioxide is achieved, and the black water after removing the acid gases enters a clarifying tank or a gray water tank after being cooled to remove solid particles and then is recycled and returned to the system for reuse; the above conventional treatment process has the following drawbacks: 1. the inlet temperature of the vacuum flash tank is high, and the amount of vacuum flash steam is large, so that the amount of circulating water consumed by the vacuum flash tank is large, and the steam consumption and the power consumption of a vacuum system are high; 2. the flash evaporation gas passing through the vacuum flash tank is large in quantity, but the flash evaporation gas cannot be recycled due to low pressure and low temperature.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to overcome the defect among the prior art, and provide one kind and divide into the level four flash distillation with black grey water treatment process to the temperature of black water carries out reasonable division in the level four flash distillation, in order to reach and reduce the temperature that gets into vacuum flash tank import department, thereby realizes reducing circulating water, steam and electric quantity consumption, realizes recycle's gasification black water level four energy recovery system for flash distillation to vacuum flash distillation vapour simultaneously.
The above technical purpose of the present invention can be achieved by the following technical solutions:
the utility model provides an energy recovery system is used in black water four-stage flash evaporation of gasification, this system includes gasification black water pipeline and grey water pipe, the black water pipeline of gasification links to each other with the lower tower import of evaporation hot water tower, and grey water pipe links to each other with the last tower import of evaporation hot water tower, and the liquid phase export of evaporation hot water tower bottom links to each other with the import of one-level low pressure flash tank, and the liquid phase export of one-level low pressure flash tank bottom links to each other with the import of second grade low pressure flash tank, and the liquid phase export of second grade low pressure flash tank bottom links to each other with the import of vacuum flash tank, the gaseous phase export of vacuum flash tank links to each other with the import of third gas-liquid knockout drum through ultra low pressure steam turbine and vacuum flash condenser, and the liquid phase export of third gas-liquid knockout drum links to each other with the lime set recovery tank, and the gaseous phase export of third gas-liquid knockout drum links to each other with the vacuum pumping system.
Preferably, a gas phase outlet at the top of the evaporation hot water tower is connected with a low-pressure steam utilization system through a first tee joint, a third end of the first tee joint is connected with an inlet of a first gas-liquid separation tank through a high-pressure flash condenser, a gas phase outlet of the first gas-liquid separation tank is connected with an acid gas torch, and a liquid phase outlet of the first gas-liquid separation tank is connected with a condensate recovery tank.
Preferably, a top gas phase outlet of the first-stage low-pressure flash tank is connected with a low-pressure steam utilization system through a second tee; the third end of the second tee is connected with the inlet of the second gas-liquid separation tank through the low-pressure steam condenser, the gas phase outlet of the second gas-liquid separation tank is connected with the acid gas torch, and the liquid phase outlet of the second gas-liquid separation tank is connected with the condensate recovery tank.
Preferably, a top gas-phase outlet of the second-stage low-pressure flash tank is connected with an inlet of a fourth gas-liquid separation tank through a tube pass of a working medium evaporator in the heat recovery unit, a gas-phase outlet of the fourth gas-liquid separation tank is connected with an acid gas torch, and a liquid-phase outlet of the fourth gas-liquid separation tank is connected with an inlet of the vacuum flash tank.
Preferably, the heat recovery unit comprises a shell side of the working medium evaporator, a shell side outlet of the working medium evaporator is connected with a shell side of the working medium condenser through an expansion generator set, and a shell side outlet of the working medium condenser is connected with a shell side inlet of the working medium evaporator through a working medium pump.
Preferably, the liquid phase outlet at the bottom of the vacuum flash tank is connected with the inlet of the clarifying tank.
Preferably, the middle part of the evaporation hot water tower is provided with a partition plate with an air cap, a hot water outlet is formed in the evaporation hot water tower on one side of the upper part of the partition plate, and the hot water outlet is connected with a high-temperature hot water storage tank through a pipeline.
Preferably, the condensate recovering tank is connected with an inlet of the clarifying tank.
According to the energy recovery system for the four-stage flash evaporation of the gasified black water, which is manufactured according to the scheme, the temperature of the black water can be reduced to 60-80 ℃ from 230-240 ℃ by arranging the evaporation hot water tower, the primary low-pressure flash evaporation tank, the secondary low-pressure flash evaporation tank and the vacuum flash evaporation tank, wherein the temperature of the black water entering the vacuum flash evaporation tank can be reduced to 100-112 ℃ from 125-140 ℃ originally by arranging the secondary low-pressure flash evaporation tank, and the flash evaporation gas quantity in the vacuum flash evaporation tank can be reduced to 1/4-1/3 of the original scale after the temperature of the black water is reduced. An ultra-low pressure turbine is arranged at a gas phase outlet of the vacuum flash tank, the exhaust pressure of the ultra-low pressure turbine is from-85 Kpa to-95 Kpa, and the vacuum flash steam at the outlet of the turbine is cooled and depressurized and has part of steam condensed, so that the pressure energy and the heat energy of the vacuum flash steam are recovered; the energy-saving and energy-saving recycling system has the advantages of simple structure, reasonable design, energy conservation, consumption reduction and energy recycling on the premise of ensuring the normal and stable operation of the whole system.
Drawings
In order to more clearly illustrate the technical solutions in the embodiments of the present invention, the drawings needed to be used in the description of the embodiments will be briefly described below, and it is obvious that the drawings in the following description are only some embodiments of the present invention, and it is obvious for those skilled in the art to obtain other drawings without creative efforts.
Fig. 1 is a schematic structural diagram of the present invention.
In the upper diagram:
1. a gasification black water pipeline; 2. an evaporation hot water tower; 3. a grey water conduit; 4. a high temperature hot water storage tank; 5. a first-stage low-pressure flash tank; 6. a low pressure steam utilization system; 7. a high-pressure flash condenser; 8. a first gas-liquid separation tank; 9. a low pressure steam condenser; 10. a second knock-out pot; 11. acid gas torch; 12. a secondary low-pressure flash tank; 13. a working medium evaporator; 14. an expansion generator set; 15. a working medium condenser; 16. a working medium pump; 17. a vacuum flash tank; 18. an ultra low pressure turbine; 19. a vacuum flash condenser; 20. a third gas-liquid separation tank; 21. a vacuum pumping system; 22. a condensate recovery tank; 23. a clarifying tank; 24. a fourth gas-liquid separation tank; 25. a first tee joint; 26. a second tee joint; 27. a separator.
Detailed Description
The technical solution of the present invention will be clearly and completely described below with reference to the specific embodiments. It is obvious that the described embodiments are only some of the embodiments of the present invention, and not all of them. Based on the embodiments of the present invention, all other embodiments obtained by a person of ordinary skill in the art without creative efforts belong to the protection scope of the present invention.
Referring to fig. 1, the utility model relates to an energy recovery system is used in flash distillation of gasification black water level four, this system is including gasification black water pipeline 1 and grey water pipe 3, gasification black water pipeline 1 links to each other with the lower tower import of evaporation hot water tower 2, and grey water pipe 3 links to each other with the last tower import of evaporation hot water tower 2, and the liquid phase export of evaporation hot water tower 2 bottom links to each other with the import of one-level low pressure flash tank 5, and the liquid phase export of one-level low pressure flash tank 5 bottom links to each other with the import of second grade low pressure flash tank 12, and the liquid phase export of second grade low pressure flash tank 12 bottom links to each other with the import of vacuum flash tank 17, the gaseous phase export of vacuum flash tank 17 links to each other with the import of third gas-liquid separation jar 20 through ultra low pressure steam turbine 18 and vacuum flash condenser 19, and the liquid phase export of third gas-liquid separation jar 20 links to each other with condensate recovery tank 22, and the gaseous phase export of third gas-liquid separation jar 20 links to each other with evacuation system 21. The utility model discloses an above-mentioned setting can change traditional second grade flash distillation or tertiary flash distillation into the level four flash distillation that comprises evaporation hot water tower 2, one-level low pressure flash tank 5, second grade low pressure flash tank 12 and vacuum flash tank 17, and above-mentioned level four flash distillation can carry out reasonable adjustment to the temperature of black water, makes the temperature threshold value of above-mentioned level four flash distillation export 170-185 ℃, 125-140 ℃, 100-112 ℃ and 60-80 ℃ in proper order; the temperature of the black water which enters the vacuum flash tank 17 originally is reduced to 100-112 ℃ from 125-140 ℃, so that the gas amount of the vacuum flash is reduced to 1/4-1/3 of the original gas amount. Meanwhile, the utility model can realize the stable operation of the ultra-low pressure turbine 18 and the third gas-liquid separation tank 20 by arranging the vacuum pumping system 21; the ultra-low pressure turbine 18 in the utility model can be directly purchased in the market, the air inlet pressure of the ultra-low pressure turbine 18 is-50 KPa to-70 KPa, and the exhaust pressure is-85 KPa to-95 KPa; the ultra low pressure turbine 18 is a conventional steam turbine, and is called an ultra low pressure turbine because the application pressure in the system is lower, and the difference between the ultra low pressure turbine 18 and the conventional steam turbine is only the difference between the inlet pressure and the exhaust pressure; the utility model discloses in evacuation system 21 include equipment and device such as water ring vacuum pump.
Further, a gas phase outlet at the top of the evaporation hot water tower 2 is connected with the low-pressure steam utilization system 6 through a first tee 25, a third end of the first tee 25 is connected with an inlet of a first gas-liquid separation tank 8 through a high-pressure flash condenser 7, a gas phase outlet of the first gas-liquid separation tank 8 is connected with an acid gas torch 11, and a liquid phase outlet of the first gas-liquid separation tank 8 is connected with a condensate recovery tank 22. The utility model discloses in the steam taste that the gaseous phase export at 2 tops of evaporation hot water tower be high, the temperature is high, its application scope is wider, can send into low pressure steam and utilize system 6 in, low pressure steam utilizes system 6 to include but not be limited to equipment or devices such as oxygen-eliminating device, strip tower, heater, evaporimeter.
Further, a top gas phase outlet of the primary low-pressure flash tank 5 is connected with the low-pressure steam utilization system 6 through a second tee 26; the third end of the second tee joint 26 is connected with the inlet of the second gas-liquid separation tank 10 through the low-pressure steam condenser 9, the gas-phase outlet of the second gas-liquid separation tank 10 is connected with the acid gas torch 11, and the liquid-phase outlet of the second gas-liquid separation tank 10 is connected with the condensate recovery tank 22. The steam at the top gas phase outlet of the primary low-pressure flash tank 5 has high taste and temperature, and wide application range, and can be sent to a low-pressure steam utilization system 6, wherein the low-pressure steam utilization system 6 comprises equipment or devices such as but not limited to deaerators, stripping towers, heaters, evaporators and the like.
Further, a top gas-phase outlet of the second-stage low-pressure flash tank 12 is connected with an inlet of a fourth gas-liquid separation tank 24 through a tube pass of a working medium evaporator 13 in the heat recovery unit, a gas-phase outlet of the fourth gas-liquid separation tank 24 is connected with an acid gas torch 11, and a liquid-phase outlet of the fourth gas-liquid separation tank 24 is connected with an inlet of the vacuum flash tank 17. The temperature and the pressure of the flash steam at the top gas phase outlet of the secondary low-pressure flash tank 12 in the utility model are lower, so that the flash steam is recovered by the heat recovery unit; the utility model discloses in the heat recovery unit include working medium evaporimeter 13's shell side, working medium evaporimeter 13's shell side export links to each other through expansion generator set 14 and working medium condenser 15's shell side, working medium condenser 15's shell side export links to each other through working medium pump 16 and working medium evaporimeter 13's shell side import.
Further, the liquid phase outlet at the bottom of the vacuum flash tank 17 is connected with the inlet of a clarifier 23.
Furthermore, a partition plate 27 with an air cap is arranged in the middle of the evaporation hot water tower 2, a hot water outlet is formed in the evaporation hot water tower 2 on one side of the upper portion of the partition plate 27, and the hot water outlet is connected with the high-temperature hot water storage tank 4 through a pipeline.
Further, the condensate recovering tank 22 is connected to an inlet of the settling tank 23.
The utility model discloses a theory of operation does: black water in the gasified black water pipeline 1 enters an evaporation hot water tower 2 to be subjected to lower tower pressure reduction flash evaporation, gray water in the gray water pipeline 3 enters an evaporation hot water tower 2 to be heated, high-temperature hot water discharged from a middle tower of the evaporation hot water tower 2 enters a high-temperature hot water storage tank 4, steam at the top of the evaporation hot water tower 2 is sent to a low-pressure steam utilization system 6 or is cooled by a high-pressure flash condenser 7 to enter a first gas-liquid separation tank 8 for gas-liquid separation, separated acid gas enters an acid gas torch 11 for combustion treatment, and separated liquid enters a condensate recovery tank 22; the bottom liquid discharged from the lower tower of the evaporation hot water tower 2 enters a first-stage low-pressure flash tank 5 for reduced pressure flash evaporation, the steam at the top of the first-stage low-pressure flash tank 5 is sent to a low-pressure steam utilization system 6, or is cooled by a low-pressure steam condenser 9 and enters a second gas-liquid separation tank 10, the separated acid gas enters an acid gas torch 11 for combustion treatment, and the separated liquid enters a condensate recovery tank 22; the bottom liquid in the primary low-pressure flash tank 5 enters a secondary low-pressure flash tank 12 for reduced pressure flash evaporation, the steam at the top of the secondary low-pressure flash tank 12 enters a fourth gas-liquid separation tank 24 for gas-liquid separation after heat exchange and temperature reduction condensation of a tube pass of a working medium evaporator 13, the separated acid gas enters an acid gas torch 11 for combustion treatment, the separated liquid enters a vacuum flash tank 17 for vacuum flash evaporation, the bottom liquid in the secondary low-pressure flash tank 12 enters the vacuum flash tank 17 for reduced pressure flash evaporation, and the bottom liquid in the vacuum flash tank 17 is discharged into a clarifying tank 23; in the process, the organic working medium is subjected to heat exchange and evaporation in the working medium evaporator 13 to be a gas phase, the gas phase enters the expansion generator set 14 to recover energy, the pressure of the organic working medium is reduced, the gas phase enters the shell pass of the working medium condenser 15 to be cooled and condensed, and the condensed liquid phase organic working medium is boosted by the working medium pump 16 and is sent to the shell pass of the working medium evaporator 13 to form circulation; in the process, steam at the top of the vacuum flash tank 17 enters an ultra-low pressure steam turbine 18 to recover energy and then enters a vacuum flash condenser 19, the steam enters a third gas-liquid separation tank 20 to be subjected to gas-liquid separation after being cooled, gas phase at the top of the third gas-liquid separation tank 20 is pumped out through a vacuum pumping system 21, and bottom liquid of the third gas-liquid separation tank 20 enters a condensate recovery tank 22.
The utility model discloses specific working procedure as follows: the method comprises the following steps: black water in the gasified black water pipeline 1 enters an evaporation hot water tower 2 to be subjected to reduced pressure flash evaporation, gray water in the gray water pipeline 3 enters an evaporation hot water tower 2 to be heated, hot water is discharged from a hot water outlet of the evaporation hot water tower 2 and is sent into a high-temperature hot water storage tank 4 through a pipeline; the pressure of the gasified black water 1 is 4.0-8.7 MPa, and the temperature is 220-245 ℃; the tower pressure below the evaporation hot water tower 2 is 0.7-1.0 MPa; step two: in the first step, the steam at the top of the hot water tower 2 is evaporated and sent to a low-pressure steam utilization system 6. The steam utilization system 6 includes, but is not limited to, deaerator, stripper, heater, evaporator, and the like. When the system is in a starting stage, the temperature of steam at the top of the evaporation hot water tower 2 is reduced by a high-pressure flash condenser 7, the steam is sent into a first gas-liquid separation tank 8 for gas-liquid separation, the separated acid gas enters an acid gas torch 11, and the separated liquid enters a condensate recovery tank 22. Step three: the bottom liquid of the evaporation hot water tower 2 in the step one enters a first-stage low-pressure flash tank 5 for reduced pressure flash evaporation; the pressure of the primary low-pressure flash tank 5 is 0.15-0.3 MPa; the steam at the top of the primary low-pressure flash tank 5 is sent to a low-pressure steam utilization system 6; when the system is in a starting stage, the steam at the top of the first-stage low-pressure flash tank 5 is cooled through the low-pressure steam condenser 9 and enters the second gas-liquid separation tank 10 for gas-liquid separation, the separated acid gas enters the acid gas torch 11 for combustion, and the separated liquid enters the condensate recovery tank 22. Step four: the bottom liquid of the first-stage low-pressure flash tank 5 in the third step enters a second-stage low-pressure flash tank 12 for reduced pressure flash evaporation; the steam on the top of the secondary low-pressure flash tank 12 enters a fourth gas-liquid separation tank 24 after being cooled and condensed on the tube pass of the working medium evaporator 13, the separated acid gas enters an acid gas torch 11, and the separated liquid enters a vacuum flash tank 17; the pressure of the secondary low-pressure flash tank 12 is 0.01-0.05 MPa; step five: the shell side of the working medium evaporator 13 is connected with an outlet of the working medium pump 16, the organic working medium is heated and evaporated at the shell side of the working medium evaporator 13, then enters the expansion generator set 14 for energy recovery, the pressure of the organic working medium is reduced after energy recovery, then the organic working medium enters the working medium condenser 15 for cooling and condensation at the shell side, and the liquid organic working medium is boosted by the working medium pump 16 and sent into the shell side of the working medium evaporator 13. The outlet pressure of the working medium pump 16 is 0.8-1.2 MPa, and the shell side pressure of the working medium evaporator 13 is 0.75-1.15 MPa. The working medium state at the outlet of the working medium evaporator 13 is a saturated steam state. The outlet pressure of the expansion generator 14 is 0.20-0.45 MPa, the temperature of the organic working medium at the outlet of the working medium condenser 15 shell side is 35-60 ℃, and the tube side of the working medium condenser 15 is circulating water; the organic working medium can be pentafluoropropane. Step six: the bottom liquid of the secondary low-pressure flash tank 12 enters a vacuum flash tank 17 for decompression flash evaporation, and the bottom liquid of the vacuum flash tank 17 is discharged into a clarifying tank 23 for repeated use; the top pressure of the vacuum flash tank 17 is-50 to-70 Kpa; step seven: steam at the top of the vacuum flash tank 17 enters an ultra-low pressure turbine 18 to recover energy, then enters a vacuum flash condenser 19, and enters a third gas-liquid separation tank 20 to carry out gas-liquid separation after being cooled; the gas phase separated from the third gas-liquid separation tank 20 is discharged out of the system through a vacuum pumping system 21, and the bottom liquid of the third gas-liquid separation tank 20 enters a condensate recovery system 22; the vacuum system 21 includes a water ring vacuum pump and other devices and apparatuses. According to the above, the utility model discloses a set up level four flash distillation process, cooperation steam utilizes system 6, heat recovery unit and ultralow pressure steam turbine 18, can be in different temperature and pressure stages according to the black water to carry out tertiary recycle to this characteristics, with the characteristics that realize improving recovery efficiency and reduce black water treatment cost.
Although embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that various changes, modifications, substitutions and alterations can be made in these embodiments without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents.
Claims (8)
1. The utility model provides an energy recuperation system for gasification black water level four flash distillation, this system includes gasification black water pipeline (1) and grey water pipeline (3), its characterized in that: the device is characterized in that a gasified black water pipeline (1) is connected with a lower tower inlet of an evaporation hot water tower (2), a grey water pipeline (3) is connected with an upper tower inlet of the evaporation hot water tower (2), a liquid phase outlet at the bottom of the evaporation hot water tower (2) is connected with an inlet of a first-stage low-pressure flash tank (5), a liquid phase outlet at the bottom of the first-stage low-pressure flash tank (5) is connected with an inlet of a second-stage low-pressure flash tank (12), a liquid phase outlet at the bottom of the second-stage low-pressure flash tank (12) is connected with an inlet of a vacuum flash tank (17), a gas phase outlet of the vacuum flash tank (17) is connected with an inlet of a third gas-liquid separation tank (20) through an ultra-low pressure turbine (18) and a vacuum flash condenser (19), a liquid phase outlet of the third gas-liquid separation tank (20) is connected with a condensate recovery tank (22), and a gas phase outlet of the third gas-liquid separation tank (20) is connected with a vacuum pumping system (21).
2. The energy recovery system for the four-stage flash evaporation of the gasified black water as claimed in claim 1, wherein: the gas phase outlet at the top of the evaporation hot water tower (2) is connected with the low-pressure steam utilization system (6) through a first tee joint (25), the third end of the first tee joint (25) is connected with the inlet of a first gas-liquid separation tank (8) through a high-pressure flash condenser (7), the gas phase outlet of the first gas-liquid separation tank (8) is connected with an acid gas torch (11), and the liquid phase outlet of the first gas-liquid separation tank (8) is connected with a condensate recovery tank (22).
3. The energy recovery system for the four-stage flash evaporation of the gasified black water as claimed in claim 1, wherein: the top gas phase outlet of the primary low-pressure flash tank (5) is connected with a low-pressure steam utilization system (6) through a second tee joint (26); the third end of the second tee joint (26) is connected with the inlet of a second gas-liquid separation tank (10) through a low-pressure steam condenser (9), the gas-phase outlet of the second gas-liquid separation tank (10) is connected with an acid gas torch (11), and the liquid-phase outlet of the second gas-liquid separation tank (10) is connected with a condensate recovery tank (22).
4. The energy recovery system for the four-stage flash evaporation of the gasified black water as claimed in claim 1, wherein: and a top gas-phase outlet of the second-stage low-pressure flash tank (12) is connected with an inlet of a fourth gas-liquid separation tank (24) through a tube pass of a working medium evaporator (13) in the heat recovery unit, a gas-phase outlet of the fourth gas-liquid separation tank (24) is connected with an acid gas torch (11), and a liquid-phase outlet of the fourth gas-liquid separation tank (24) is connected with an inlet of a vacuum flash tank (17).
5. The energy recovery system for the four-stage flash evaporation of the gasified black water as claimed in claim 4, wherein: the heat recovery unit comprises a shell pass of the working medium evaporator (13), a shell pass outlet of the working medium evaporator (13) is connected with a shell pass of the working medium condenser (15) through an expansion generator set (14), and a shell pass outlet of the working medium condenser (15) is connected with a shell pass inlet of the working medium evaporator (13) through a working medium pump (16).
6. The energy recovery system for the four-stage flash evaporation of the gasified black water as claimed in claim 1, wherein: and a liquid phase outlet at the bottom of the vacuum flash tank (17) is connected with an inlet of a clarifying tank (23).
7. The energy recovery system for the four-stage flash evaporation of the gasified black water as claimed in claim 1, wherein: the middle part of the evaporation hot water tower (2) is provided with a clapboard (27) with an air cap, a hot water outlet is arranged on the evaporation hot water tower (2) at one side of the upper part of the clapboard (27), and the hot water outlet is connected with a high-temperature hot water storage tank (4) through a pipeline.
8. The energy recovery system for the four-stage flash evaporation of gasified black water according to claim 2, 3 or 6, wherein: the condensate recovery tank (22) is connected with an inlet of the clarifying tank (23).
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| Application Number | Priority Date | Filing Date | Title |
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| CN202222604311.1U CN218106766U (en) | 2022-09-29 | 2022-09-29 | Energy recovery system for gasification black water four-stage flash evaporation |
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| CN202222604311.1U CN218106766U (en) | 2022-09-29 | 2022-09-29 | Energy recovery system for gasification black water four-stage flash evaporation |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN118059522A (en) * | 2024-04-22 | 2024-05-24 | 万华化学集团股份有限公司 | Method and system for heat recovery of coal chemical industry gasified black water |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN118059522A (en) * | 2024-04-22 | 2024-05-24 | 万华化学集团股份有限公司 | Method and system for heat recovery of coal chemical industry gasified black water |
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| GR01 | Patent grant | ||
| GR01 | Patent grant |